MX2008013524A

MX2008013524A - Co-polyester packaging resins prepared without solid-state polymerization, a method for processing the co-polyester resins with reduced viscosity change, and containers and other articles prepared by the process.

Info

Publication number: MX2008013524A
Application number: MX2008013524A
Authority: MX
Inventors: Peter S Kezios; Helen Codd; Kevin Richard Harrison
Original assignee: Dak Americas Llc
Priority date: 2006-04-21
Filing date: 2007-04-20
Publication date: 2009-01-26
Also published as: BRPI0710634B1; AU2007240369A1; BRPI0710634A2; PT2013005T; EP2013005A2; RU2008145894A; CA2648815C; CN101448633A; CN101448633B; EP2013005B1; NO343880B1; EP2013005A4; WO2007124428A2; NO20084404L; WO2007124428A3; ES2884216T3; KR20080110927A; JP2009534227A; CA2648815A1; US20070248778A1

Abstract

A method of processing a polyester composition without changing the Intrinsic viscosity of the polyester polymer by more than 0.025 dL/g such as Injection molding a PET resin to form a bottle perform and blow molding a container from the bottle preform.

Description

CO-POLYESTER PACKING RESINS PREPARED WITHOUT POLYMERIZATION IN A SOLID STATE, A METHOD FOR PROCESSING CO-POLYESTER RESINS WITH A REDUCED VISCOSITY CHANGE. AND CONTAINERS AND OTHER ARTICLES PREPARED THROUGH THE PROCESS BACKGROUND OF THE INVENTION FIELD OF THE INVENTION The invention relates to a method for processing a polyester resin, which includes melting and subsequently solidifying the polyester resin to form a shaped article without decreasing the intrinsic viscosity of the polyester resin by more. of 0.025 deciliters / gram. The invention further relates to molded articles prepared by the method, and to polyester resins capable of undergoing processing without a decrease in intrinsic viscosity of more than 0.025 deciliters / gram. DESCRIPTION OF THE RELATED ART Polyester resins, including resins such as poly- (ethylene terephthalate) (PET), poly- (butylene terephthalate) (PBT), poly- (ethylene naphthalate) (PEN), poly- (trimethylene terephthalate) (PTT), and poly- (trimethylene naphthalate) (PTN), are conventionally used as resins in the manufacture of containers, such as beverage bottles. The properties, such as flexibility, good impact resistance, and transparency, together with good melt processability, allow the resins to This policy is widely used for this application. The term "resin", as used herein, includes all of the aforementioned materials. The starting feedstocks for polyester resins are petroleum derivatives, such as ethylene, which are obtained from petroleum or natural gas, and para-xylene, which is typically obtained from petroleum. Polyester resins are generally made by a combined esterification / polycondensation reaction between monomeric units of a diol (eg, ethylene glycol (EG)) and a dicarboxylic acid (eg, terephthalic acid (TPA)). The terms "carboxylic acid" and / or "dicarboxylic acid", as used herein, include those derived from carboxylic acid ester and dicarboxylic acid. The esters of carboxylic acids and dicarboxylic acids may contain one or more alkyl groups of 1 to 6 carbon atoms (for example, methyl, ethyl, propyl, isopropyl, butyl, isobutyl, tertiary butyl, pentyl, hexyl, and mixtures thereof) in the ester unit, for example, dimethyl terephthalate (DMT). In conventional esterification / polycondensation processes, the polyester can be formed, for example, by first producing a prepolymer of a low molecular weight and a low intrinsic viscosity (IV) (eg, a mixture of oligomers), for example, by the reaction of a diol and a dicarboxylic acid in a reaction in the melting phase. The formation of oligomers can be carried out by the reaction of an aqueous phase of diol and monomeric units of dicarboxylic acid in an esterification reactor. The ethylene glycol can be lost towards evaporation during the esterification reaction, which can be carried out at high temperatures. Accordingly, the aqueous slurry of diol and dicarboxylic acid may contain an excess of ethylene glycol, for example the diol and the dicarboxylic acid may be present in a molar ratio of about 1.2 to about 2.5, based on the total glycol to the total diacid. The additional pre-polycondensation and polycondensation of the oligomers can be carried out to provide a resin mixture with an intrinsic viscosity of 0.50 to 0.65. These resin blends are suitable in different applications, such as fibers / filaments, fiber fragments, or resin precursors for bottles. Amorphous transparent base fragments having an intrinsic viscosity of 0.50 to 0.65 can be subjected to solid state polymerization (SSP) to increase molecular weight (e.g., up to an intrinsic viscosity of 0.74 to 0.76 for water bottle applications, from 0.83 to 0.85 for CSD / beer bottles, etc.). The solid state polymerization process (SSP) unit can result in the resin undergoing crystallization, which forms opaque granules. A continuous polycondensation process in the polyester melting phase usually consists of three reaction steps: (i) esterification to form low molecular weight oligomers, (ii) prepolymerization of the oligomers to form a pre-polymer, and (ij) polycondensation to form a polymer with an intermediate molecular weight or intrinsic viscosity (eg, an intrinsic target viscosity of 0.50 to 0.65). The three reaction steps (i), (i), and (iii) above can be carried out to achieve the intrinsic target viscosity in 2 to 6 reactors, using the existing melt-phase process technology. In general, the esterification is conducted in one or two containers to form a mixture of low molecular weight oligomers with a low degree of polymerization (for example, up to about 7 pairs of reactive monomer units). The oligomers are then pumped into one or two pre-polymerization vessels, where higher temperatures and lower pressures help to remove water and ethylene glycol. The degree of polymerization is then increased to a level of 15 to 20 repeating units. The temperatures are further increased, and the pressures are further reduced, in the one or two final containers, to form a polymer ready to be cut into granules, for example, or to be spun directly into fibers or filaments. The esterification and pre-polymerization vessels can be stirred. Polycondensation containers (eg, terminators, cleaned film reactors, etc.) may have agitators designed to generate very thin films. The temperatures and holding times are optimized for each set of containers, in order to minimize degradation and other secondary reactions. Some by-products that can be generated by the melt-phase reaction of polyester include diethylene glycol (DEG), acetaldehyde, water, cyclic oligomers, carboxyl end groups, vinyl end groups, and anhydride end groups. Both time and temperature are two variables that are preferably controlled during an esterification / polycondensation reaction. With higher reaction temperatures, the total reaction time is reduced significantly, and less residence time and / or fewer reactors are needed. Alternatively, for this continuous production method, the polyesters can be prepared using a batch method. In a batch method, the diol and dicarboxylic acid units are mixed together in a single reactor. In some cases, more than one reactor (for example, reaction vessel) may be used if necessary. The diol / dicarboxylic acid mixture is heated to cause the monomer units to undergo a condensation reaction. The byproducts of the condensation reaction may include water or an alcohol. By conducting the reaction under reduced pressure, or by subjecting the reaction mixture under reduced pressure during the final stages of the reaction, the volatile byproducts of the reaction can be removed, thereby promoting the reaction until finished. Certain physical and chemical properties of polymeric materials are adversely affected by long exposure to elevated temperature, especially if the exposure is in an atmosphere containing oxygen, or at temperatures greater than, say, 250 ° C. Conventional methods for the preparation of polyester resins, such as PET, may suffer from the drawbacks associated with the need to carry out a solid state polymerization (SSP), which subjects the resin to a long heating history, and / or may require high capital expenditure. The production of a polyester resin, such as PET, can be carried out directly from a melting phase of the monomer units, without any polymerization in the final solid state. For example, you can carry a batch process at a sufficient temperature, for a sufficient time, and at a sufficient pressure, to drive the polycondensation reaction to completion, thus avoiding the need for a subsequent finish (e.g., final reaction). Polycondensation in the solid state is an important step in some conventional processes used to make high molecular weight polyester resins for applications in bottles, food trays, and tire ropes. Transparent amorphous granules (with an intrinsic viscosity of 0.50 to 0.65) produced by the polycondensation reaction processes Conventional melts can be further polymerized in the solid state at a temperature substantially higher than the glass transition temperature of the resin, but below the crystalline melting point of the resin. The polymerization in the solid state is carried out in a stream of an inert gas (usually nitrogen under continuous operation), or under vacuum (usually in a rotary vacuum drier in batches). At an appropriate solid state polymerization temperature, the functional end groups of the polymer chains (e.g., PET) are sufficiently mobile, and react with each other to further increase the molecular weight. A conventional process for producing polyester resins for container applications, including melt phase polycondensation and solid state polymerization, wherein the monomeric components of a polyester resin, such as PET, is shown schematically in Figure 1 is shown schematically. they are mixed in an esterification / polycondensation reactor in the melting phase. The reaction is carried out to provide a molten resin having an intrinsic viscosity (IV) of 0.5 to 0.65. The molten product obtained by the esterification / polycondensation in the melting phase is then subjected to a filtration of the polymer. Optionally, a co-barrier resin can be added to the molten and filtered polymer, by extruding the co-barrier resin and adding to the extrudate the molten and filtered resin obtained from the esterification / polycondensation in the fusion. The mixed streams, or the polyester stream obtained from the filtration of the polymer, can then be pumped into a mixer. A static mixer can be used to ensure that the polyester resin and any co-barrier resin are sufficiently mixed. Sterification / polycondensation in the melting phase is typically carried out in a plurality of reactors. Accordingly, the monomers can be added to a first esterification reactor to form a material of low intrinsic viscosity. As the oligomers pass through the remaining reactors, the intrinsic viscosity subsequently rises as the polycondensation reaction proceeds sequentially through a series of reactors. The material in molten form that is pumped from the static mixer is subjected to solidification and granulation. The molten material can be solidified by passing the strands or filaments of the formed material, by pumping the material through, for example, a die with a series of holes. As the molten polyester resin is passed through a hole, a continuous strand is formed. As the strands pass through water, the strands are immediately cooled to form a solid. Subsequent cutting of the strands provides granules or fragments which, in a conventional process, are then transferred to a solid state polymerization stage (i.e., SSP). In conventional processes for the preparation of resins of polyester, and even in some processes that avoid the use of a polymerization in solid state after the polymerization is completed, the polymerized molten resin can be pumped through a die to form multiple strands. The molten resin that comes out of the die is quickly quenched in water to harden the resin. As a result of rapid cooling (eg, quenching with water), the molten polyester has no time to crystallize, and solidifies in an amorphous state. The solidified polyester strands, or the granules derived from the cut strands, are clear, transparent, and are in an amorphous state. The polymerization in the solid state can include several reactors and / or individual processing stations. For example, solid state polymerization may include a pre-crystallization step, wherein the fragments and / or granules are transformed from an amorphous phase to a crystalline phase. The use of a polyester resin in the crystalline phase is important in the last steps of the solid state polymerization, because the use of amorphous polyester fragments can result in the formation of lumps of the granules, because a resin polyester in amorphous state may not be sufficiently resistant to adhesion between the granules and / or fragments. The solid state polymerization process further includes a crystallizer (eg, crystallization step), a preheater, a cooler, and a solid state polymerization reactor.

Some manufacturing processes do not include a solid state polymerization. The processing of a polyester resin directly from a melt-phase condensation to obtain pre-forms for blow molding applications is described in U.S. Patent No. 5,968,429 (incorporated herein by reference). In its whole). The polymerization is carried out without an intermediate solidification of the melting phase, and allows the continuous production of molded polyester articles (eg, pre-forms) from a continuous melt phase reaction of the starting monomers. After pre-crystallization, the fragments and / or granules can be subjected to a final crystallization. A final crystallization may include, for example, the appropriate heating of the fragments (spheres, pellets, granules, round particles, etc.) at the appropriate temperatures. Once the polyester resin is in a crystallized state, the granules and / or fragments are preheated and ready to be transferred to the top of a polymerization reactor in the solid state to counter-flow (parallel to the pre-heater). ), by means of a pneumatic system (for example, Buhler technology). If an inclined crystallizer is stacked on the solid state polymerization reactor, then the hot / crystallized fragments enter the polymerization reactor in the solid state by means of the rotating screw of the crystallizer (for example, Sinco technology). The solid state polymerization reactor is can consider as a moving bed of fragments that move under the influence of gravity. The fragments have a slow downward flow rate of 30 to 60 millimeters / minute, and the nitrogen has a high upward flow velocity of about 18 meters / minute. A typical mass-flow ratio of nitrogen to PET is in the range of 0.4 to 0.6. In a gravity flow reactor, the granules and / or fragments are subjected to elevated temperatures for periods of up to 15 hours. Heating and flushing with nitrogen through the gravity flow reactor will drive the polycondensation reaction, and will result in longer chain lengths, and in a concurrent manner, a higher intrinsic viscosity of the resins. After passing through the gravity flow reactor, granules and / or fragments of a wide range of intrinsic viscosities can be formed, for example, with an average intrinsic viscosity of about 0.84 deciliters / gram, for example, for CSD / beer . The granules and / or fragments have an opaque characteristic due to their crystallinity. The crystalline material is transferred to a product silo for storage and / or packaging. The finished product in the crystalline state, and having an intrinsic viscosity of about 0.84 deciliters / gram, for example for CSD / beer, can be further mixed with other co-barrier resins (powders, granules, spheres, pellets, etc.). ) by the molders or processors that acquire the resins of polyester for the manufacture, for example, of bottles and / or containers. Accordingly, in a conventional process, a melt-phase polycondensation process can be employed to make transparent amorphous granules (typically of intrinsic viscosity from 0.5 to 0.65) as precursors for the bottle resins. The amorphous granules are first pre-crystallized, crystallized, and / or preheated, then subjected to polymerization in the solid state in a gravity flow reactor (for example, a non-agitated reactor). After crystallization, the resin granules become opaque, and do not adhere to each other, if the temperature of the polymerization in the solid state is at least 10 ° C below the setting of the melting temperature of the resin granules. In a process of fusion of high intrinsic direct viscosity, only the melting process is used (without solid state polymerization) to make a variety of bottle resins (for example, an intrinsic viscosity of 0.72 to 0.78 for water bottles, an intrinsic viscosity of 0.83 to 0.87 for bottles for CSD / beer), as desired. In a high intrinsic direct viscosity melting process, a terminator (eg, a cleaned film or thin film evaporator) can be used to effectively and quickly remove reaction byproducts, such as ethylene glycol (major) , water, acetaldehyde, etc. The immediate removal of ethylene glycol / water under high temperatures drives the balance of the polycondensation reaction towards the polymer side. It is known that PET or other polyester resins have a hygroscopic behavior (for example, they absorb water from the atmosphere), in such a way that the granules obtained by cutting off strands with water contain significant amounts of water. Conventionally, the granules can be dried by passing dry air over the granules, or by heating. Heating for a prolonged period at an elevated temperature can lead to problems, because amorphous polyester granules (eg, PET) may tend to adhere to one another. In the preform molding processes, the granules and / or fragments are typically dried prior to molding. After proper drying, the granules and / or fragments may have a water content of not more than 50 parts per million. The fragments and / or the granules are then processed, for example, in the form of preforms, by injection molding. Because residual water is present in the resin during the injection molding process that is carried out at elevated temperatures (for example, at temperatures above 200 ° C), the intrinsic viscosity of the resin can be reduced, for example , by hydrolytic degradation. The starting fragments can be of an intrinsic viscosity of about 0.84. The intrinsic viscosity in the following injection molded preforms formed from the starting resin may have an intrinsic viscosity of about 0. 80. Accordingly, an approximate reduction of 5 percent in the intrinsic viscosity of about 0.04 deciliters / gram in the passage from the fragments and / or granules to the preform prepared by injection molding can occur, when the fragments and / or granules have dried properly and contain at most approximately 50 parts per million water. The polyester material containing a large amount of water can undergo thermal and hydrolytic degradation. Excess water in the resin can lead to a substantial reduction in intrinsic viscosity of 30 percent or more. In order to take into account the loss (for example, reduction) in the intrinsic viscosity that occurs during processing, a resin having an intrinsic viscosity higher than the intrinsic viscosity desired for the final product must be manufactured. Typically, the difference in intrinsic viscosity in the resin before forming a preform, and the intrinsic viscosity of the resin after forming the preform, is from about 0.03 to 0.05 deciliters / gram. Accordingly, in order to produce a molded article having an intrinsic target viscosity of 0.80, the base resin must first be manufactured at an intrinsic viscosity of 0.83 to 0.85. Because a higher intrinsic viscosity is needed, longer polymerization times are required during the production of the base resin. Longer polymerization times result in a reduction in production capacity.

The particular mechanism by which the resin becomes reduced in intrinsic viscosity during processing is not known, but it is generally understood that it can be attributed to one or more degradation processes, including thermal, hydrolytic, oxidative, induced degradation. tear, or free radicals. The degradation of the resin may be accompanied by the formation of side products, such as acetaldehyde. The reduction in intrinsic viscosity observed for some polyester resins occurs when the base resin is processed. The process usually includes a step where the resin melts and / or is subjected to a high shear stress. This processing may include injection molding or other processing whereby the base resin is melted or transformed to a fluid state from a solid state, and it cools to form a solid. Methods for the processing of polyester resins that do not result in a decrease in the intrinsic viscosity of the polyester resin would be desirable, because the producer of the polyester resin can achieve higher throughput and therefore productivity. Concurrently, the resin processor (for example, injection molding) can realize higher productivity from better processing cycle times, such as injection molding cycles, because the resin with a viscosity lower initial intrinsic may require less energy to melt, and more quickly fill the molds, and / or transform into the liquid state with less shear stress in relation to the shear stress to which a resin with a higher intrinsic viscosity can be exposed during processing. Processing may include other types of processes with or without melting, whereby the polyester resin is formed in a different form, including, for example, compression molding, stretch blow molding, thermoforming, and injection molding. reaction. Conventionally, a resin preform is transformed to a bottle or container by blow molding. The blow molding is carried out at a temperature higher than the glass transition temperature of the polyester, for example from 90 ° C to 110 ° C, which is substantially lower than the injection molding temperatures to which they are exposed. the granules and / or fragments during injection molding to form the preform. The pre-heating of a preform is often carried out by infrared heating. During blow molding, the intrinsic viscosity of the resin may not change substantially, and preferably nothing changes. BRIEF DESCRIPTION OF THE INVENTION In accordance with the foregoing, an object of the invention is to provide a method for processing a polyester resin without reducing the intrinsic viscosity of the resin by more than 0.025 deciliters / gram.

Another object of the invention is to provide a method for processing a polyester resin with less degradation than conventional processing. Another object of the invention is to provide a method for producing a carbonated soft drink bottle, which includes forming a preform from a solid polyester resin, and then forming the carbonated soft drink bottle from the preform without reducing the intrinsic viscosity of polyester resin by more than 0.025 deciliters / gram. Another object of the invention is to provide a processing method for forming solid articles from a polyester resin, using less energy, and with a faster cycle time. Another object of the invention is to provide a method for processing a polyester resin, which allows a greater amount of re-ground polyester to be present in the polyester resin, without substantially affecting the properties of the molded article prepared therefrom, compared to a molded article prepared from virgin polyester resin. Another object of the invention is to provide a molded article that is prepared by a process wherein a polyester resin is processed without a loss of more than 0.025 deciliters / gram. Another object of the invention is to provide a polyester resin having a better gas barrier resistance, which is made by a process without polymerization in solid state, and that is capable of undergoing processing with a lower degree of intrinsic viscosity reduction, with a higher amount of gas barrier additive. It is a still further object of the invention to provide a polyester resin that is capable of undergoing melting and processing, including solidification, without a significant change in intrinsic viscosity. BRIEF DESCRIPTION OF THE DRAWINGS A more complete appreciation of the invention, and of many of the advantages added thereto, will be readily obtained as it becomes better understood by reference to the following detailed description, when considered in connection with the accompanying drawings, wherein: Figure 1 shows a process for producing polyester resins, which includes polycondensation in the melting phase and polymerization in the solid state. Figure 2 shows a process for producing polyester resins without polymerization in the solid state. Figure 3 shows a comparison of the intrinsic viscosity gradient of a CSD / beer resin, made with and without solid state polymerization. Figure 4 shows a comparison of the intrinsic viscosity gradient in a water bottle resin made with and without solid state polymerization.

Figure 5 shows a bottle preform that can be a shaped article formed in an embodiment of the method of the invention. Figure 6 shows a blow molded article obtained from a shaped article obtained by an embodiment of the method of the invention. DETAILED DESCRIPTION OF THE PREFERRED MODALITIES One aspect of the invention is a method that includes processing a resin, for example, by melting the resin, forming an article configured from the molten resin, and cooling the article configured to form an article. configured solid, without changing the intrinsic viscosity (IV) of the polyester resin by more than 0.025 deciliters / gram. The processing includes any method by which the polyester resin is transformed from the solid form to a flowable and / or plastic form. The transformation may include heating the polyester resin beyond the glass transition temperature, and then forming a solid shaped article from the heated polyester resin. The processing further includes any method by which a solid polyester resin is heated above its glass transition temperature and / or its melting temperature, and subsequently and / or concurrently, is formed into a shaped article, which includes: injection molding, reaction injection molding (RIM), stretch blow molding, injection blow molding, recycling, molding extrusion, compression molding, thermoforming, and methods for processing polyester resins as described in "PET Packaging Technology," by David W. Brooks and Geoff Giles (2002), whose portions describe the processing methods for polyester resins and / or PET resins are incorporated herein by reference. Preferred processing includes injection molding (blowing), sheet and film extrusion, and compression molding. The measurement method for determining the intrinsic viscosity in solution (IV) of polyester resins (eg, PET) is conventionally known. The intrinsic viscosity in solution can be measured at a concentration of 0.50 percent of the resin, in a solution of 60/40 (weight percent / weight percent) of phenol / 1,1,2,2-tetrachloro- Ethane, by means of a glass capillary viscometer. The conditions for measuring the intrinsic viscosity in solution are described in ASTM D 4603-03 (approved March 10, 2003, and published in April 2003, incorporated herein by reference in its entirety). The intrinsic solution viscosity of the co-barrier resins described herein can also be measured by the same method used to determine the intrinsic solution viscosity for the polyester resins. The glass transition temperature of the polyester resin processed in the invention is not restricted, and can be defined or influenced by the degree of polymerization and / or the content of monomer of the polyester resin (for example, the number of polymerized monomer units forming the polymer chain), and / or the molecular weight distribution of a mixture of different polymers of different degree of polymerization (polydispersity), and / or the identity and number of monomeric or co-monomeric units of the polyester resin. Preferably, a polyester resin having a narrower molecular weight distribution is used, because it can show less degradation, and a more stable intrinsic viscosity over processing, than a polyester resin having a weight distribution broad molecular The glass transition temperature (Tg) of the resin is preferably from 75 ° C to 90 ° C, more preferably from 80 ° C to 85 ° C, and most preferably from about 82 ° C. The Tg of the resin compositions containing additives may have crystal transition temperatures higher or lower than those mentioned above, therefore as 5 ° C. In a preferred embodiment, the resin is in the form of a solid particle, and has a uniform intrinsic viscosity distribution across all the dimensions of the particles. Conventional resins in the form of solid particles made with solid state polymerization can have an intrinsic viscosity gradient when they are in the form of a fragment or a granule. A fragment or granule having an intrinsic viscosity gradient may have an intrinsic viscosity that vary through the dimension of the granule and / or fragment. For example, a particular polyester resin granule can have an intrinsic viscosity of 0.9 when measured on the outside of a granule or fragment, and an intrinsic viscosity that is different from the intrinsic viscosity measured inside the granule and / or fragment (for example, there may be an intrinsic viscosity gradient of as much as 0.2 to 0.3 deciliters / gram through the size of the fragment and / or granule). This intrinsic viscosity gradient does not normally affect the overall or average intrinsic viscosity of the polyester resin when measured in bulk. However, it can introduce variability in the determination of the intrinsic viscosity of small samples of the polyester resin, if there is an insufficient amount of polyester resin in the sample, and therefore, the sample does not provide a cross-section representative of the materials present in the granules and / or polyester fragments. The existence of the intrinsic viscosity gradient in the resin in conventional solid form can be due to the solid state polymerization during which the resin particles are heated in the solid form, and ethylene glycol can be formed and released (eg, custom-made that the resin undergoes an additional condensation and suffers chain lengthening). If ethylene glycol is slow to diffuse out of the resin, its presence may slow the chain elongation action.

It is thought that, during polymerization in the solid state, the exterior of the resin particle is subjected to a longer heat history, because it is the first portion of the resin in solid form that is to be heated in the process of polymerization in solid state. The ethylene glycol formed by the polymerization is more likely to escape from the periphery of the resin particle (eg, granule or fragment), due to a tendency to diffuse more easily out of the particle, compared to the ethylene glycol present in the particle. center of the resin particle. In contrast to conventional resins, the resin used in the process of the invention is not subjected to polymerization in the solid state, and has no or substantially no intrinsic viscosity gradient in the resin particle, or has substantially less viscosity variation intrinsic (for example, gradient) through the resin particle. The intrinsic viscosity of the resin of the invention, in one aspect of the invention, may vary by not more than 0.05, preferably by not more than 0.03, preferably by not more than 0.025, more preferably by not more than 0.02, still of more preferably by no more than 0.015, and most preferably by no more than 0.01, and most preferably, the intrinsic viscosity will be the same across any dimension of the resin particle. Figure 4 provides a comparison of the intrinsic viscosity variation in a resin grade of CSD / conventional beer in solid form, as compared to a corresponding resin according to the invention (ie, a resin that is not subjected to polymerization in the solid state). Figure 3 shows the intrinsic viscosity of the exterior of the resin particles in relation to the intrinsic viscosity measured for the resin inside the resin particle (eg, core of the granule). The intrinsic viscosity measurements represent the intrinsic viscosity measured from the samples obtained by grinding the resin particles for consecutively longer periods of time. The milling is carried out by cryo-milling, with a 1-millimeter slot container, collecting the samples every 5 seconds. When the resin in solid form is initially subjected to grinding, only small fragments and / or dust are removed from the outside of the granule. Therefore, the intrinsic viscosity measured for the powder and / or the small fragments obtained by milling for a shperiod of time, is representative of the exterior of the resin in solid form. The intrinsic viscosity is measured for this powder and / or fragment, in order to provide the data used to prepare Figure 3. Similar results are seen for a resin to be used in the manufacture of bottles for water (see Figure 4). Figures 3 and 4 show that the resin that can be used in the process of the invention has a lower intrinsic viscosity gradient compared to resins conventional In a preferred embodiment of the invention, the processing of the invention includes heating the polyester resin above its melting temperature. Further preferably, the polyester resin is heated to the point where there is a free flowing liquid. In a further preferable embodiment of the invention, the polyester resin is subjected to a high shear stress while heating. The high shear stress conditions are the conditions that can be observed or created in processes such as conventional injection and / or extrusion molding, which result in the melting and mixing of the polyester resin during processing. The processing can be carried out on a polyester resin that is dried or not dried. A dried polyester resin is a crystallized resin that has been heated in its solid state to a temperature above the glass transition temperature, in a dehumidifying medium. A dried polyester resin contains less than 1,000 parts per million, preferably less than 500 parts per million, more preferably less than 50 parts per million, and especially preferably less than 25 parts per million water, b on the weight of water in relation to the total weight of the resin. Drying can also be carried out by exposing the polyester resin to a dehumidified atmosphere, to thereby remove water adsorbed or absorbed by the polyester resin.

The non-dried polyester resin can be a polyester resin containing water, or a resin that is free of water. A resin that is free of water may be one that is obtained by solidifying a polyester resin liquid obtained directly from a polyester polymerization process, in an atmosphere that is substantially free of water (eg, substantially free). of water includes atmospheres having 99 percent, preferably 99.5 percent, more preferably 99.9 percent by volume and free of water vapor). Accordingly, a non-dried polyester resin may be one that has not been subjected to heating in the solid state. A non-dried polyester resin can be one that is obtained in the solid form from a polyester polymerization process, and then stored in an atmosphere that is not inert and / or that does not dry (e.g., dehumidified) . The water vapor present in the atmosphere can be absorbed on the surface of the polyester resin, and / or can be absorbed in the matrix of the polyester resin. A quantity of water of as much as 5 percent by weight may be present, b on the weight of the water in relation to the total weight of the resin. Preferably, the polyester resin used in the method of the invention is a non-dried water-free resin, or a dried resin. In another embodiment of the invention, the resin that is subjected to the melting and processing of the invention may be a resin that has not dried, or that has dried to a lesser extent than conventional resins (for example, resins prepared with solid state polymerization). Because the resin described herein can be processed with less change in intrinsic viscosity, for example, caused by the melting and processing of the resin, the resin can contain a relatively greater amount of water, and still provide a resin processed that has a reduction in intrinsic viscosity that is not greater than the reduction in intrinsic viscosity observed when conventional resins are processed. Accordingly, the resin of the invention does not need to be completely dried (for example, compared to the necessary drying in a conventional resin), but is still capable of providing a shaped article having an intrinsic viscosity change equivalent to, or less than, the change in viscosity (eg, reduction in intrinsic viscosity) for a conventional resin that undergoes the same fusion and processing. In a preferred embodiment, the polyester resin in solid form is dried before processing. The drying can be carried out in a conventional dryer, by passing dehumidified air over the fragments and / or the granules of the polyester resin in solid form. Preferably, the polyester resin is dried in a dehumidified environment for 2 to 10 hours, more preferably for 4 to 8 hours, and most preferably for about 6 hours. The dehumidified gas that passes over the granules and / or polyester fragments has a point of dew less than -10 ° C, preferably less than -20 ° C, more preferably less than -40 ° C, still more preferably less than -50 ° C, and most preferably less than -60 ° C. The dehumidified gas that passes over the polyester granules has a temperature in the range of 220 ° F to 400 ° F (from 104 ° C to 204 ° C), preferably from 260 ° F to 360 ° F (from 126 ° C). C at 182 ° C), and more preferably 300 ° F to 320 ° F (148 ° C to 160 ° C). By subjecting the resin to less drying, or drying the resin under conditions that do not require the temperatures and / or dew points necessary to achieve sufficient drying in conventional resins, significant savings in utility can be realized. and on equipment costs. Accordingly, in one embodiment of the invention, a resin in solid form can be subjected to melting and processing without drying, or with partial drying, and still forming a shaped article exhibiting a change in intrinsic viscosity after melting and of the processing which is not greater or less than the change in intrinsic viscosity observed under the same conditions with a corresponding conventional resin (for example, a polyester resin made with a process including solid state polymerization). The reduced drying requirements allow the design of manufacturing facilities (including the construction of new plants) with less capital investment dedicated to drying facilities and auxiliary infrastructure. The polyester resin of the method of the invention can be any polyester resin including a conventional polyester resin. Conventional polyester resins can be prepared by the reaction of the monomeric units of a diol and a carboxylic acid (or an ester of a carboxylic acid). In order to obtain a sufficient intrinsic viscosity, conventional polyester resins can be subjected to a solid state polymerization. However, some polyester resins can be made without polymerization in the solid state. In a polyester resin made without solid state polymerization, the resin produced by the polymerization reaction of one or more diol units and one or more carboxylic acid / ester units, can be used to form preforms directly from the resin of molten polyester without undergoing any intermediate solidification, or it may be solidified into fragments and remelted in order to mold preforms or other objects. Examples of the preferred polyester resins made without solid state polymerization include the resins described in U.S. Patent Application Number 11 / 294,370, incorporated by reference in its entirety. In a preferred embodiment, the resin used in the method of the invention is a resin that is prepared without polymerization in the solid state. A resin prepared without polymerization in the solid state can include a resin that is made up to its final intrinsic viscosity (for example, the viscosity that is measured on the granules or the commercially transported form), without polymerization in the solid state (for example, heating the resin in the solid state at a temperature and for a period of time sufficient to increase the intrinsic viscosity by more than 0.05 deciliters / gram). For example, the resin of the invention is made without polymerization in the solid state, and has an intrinsic viscosity substantially achieved by the polymerization of the monomer units in the molten phase. Optionally, the resin in solid form thus obtained is not subsequently heated to a temperature at which further polymerization or finishing polymerization can be achieved. In other embodiments, the resin used in the method of the invention may have a lower degree of polymerization, which is achieved at least partially by heating the resin in the solid form after it is made by melt polymerization, and is isolated in the solid phase. For example, in one embodiment, a resin used in the method of the invention can have an intrinsic viscosity of 0.7, and can be derived from a resin having an intrinsic viscosity of 0.88, achieved by performing the polymerization without the conventional solid state polymerization. However, the following handling or heating of the resin in the solid form, either through a conventional solid state polymerization, or through other means, such as drying at elevated temperature, can increase the intrinsic viscosity by a amount, for example, of 0.02 deciliters / gram. Therefore, the resin, having a final intrinsic viscosity of 0.70, is produced by first forming a resin having an intrinsic viscosity of 0.68 without polymerization in the solid state, and then increasing the intrinsic viscosity of the resin by a smaller amount (eg, 0.02 deciliters / gram) ), to prepare in this manner a resin having a final intrinsic viscosity of 0.070. Preferably, the intrinsic viscosity of the resin used in the process of the invention is increased by not more than 0.05, preferably 0.04, more preferably 0.03, still more preferably 0.02, especially preferably 0.01, and most preferably 0 deciliters / gram, after the resin is initially isolated from the melt polymerization. The term "without solid state polymerization", as used herein, includes resins which are made by melt polymerization to a first intrinsic viscosity, and then further polymerized in the solid state to a second intrinsic viscosity which is not more than 0.05 deciliters / gram greater than the first intrinsic viscosity. The intrinsic viscosity of the polyester resin that can be used in the method of the invention can fall within a wide range. For example, for containers for carbonated soft drinks, the intrinsic viscosity of the polyester resin can be from 0.6 to 1.0 deciliters / gram, preferably from 0.7 to 0.9, more preferably from 0.75 to 0.85, still more preferably from 0.77. to 0.83, and in a particularly preferable way of about 0.8. In one embodiment of the method of the invention, the intrinsic viscosity of the polyester resin changes by no more than 0.025 deciliters / gram after undergoing processing to form a solid article (e.g., melting first and then solidifying). Preferably, the change in intrinsic viscosity is not greater than 0.025, more preferably not greater than 0.02, still more preferably not greater than 0.015, most preferably the change in intrinsic viscosity is not greater than 0.01, and especially preferably there is no measurable change in the intrinsic viscosity. In one embodiment of the invention, the polyester resin is in the form of a solid (for example, a polyester resin in solid form), which is processed by melting, forming a shaped article, and then solidifying to produce an article configured. The polyester resin in initial solid form can be in the form of fragments or granules. The polyester resin in solid form may contain a re-milled or re-cycled amount of polyester, from 0 to 20 weight percent, based on the total weight of the polyester resin, and preferably the re-cycled material or re-ground is present in an amount of not more than 15 weight percent, more preferably not more than 10 weight percent, still more preferably not more than 5 weight percent, and in a highly preferred embodiment , the polyester resin in solid form is a virgin resin that does not contain re-ground or re-cycled polyester material, and is in the form of different solid particles (per example, granules and / or fragments). During the manufacture of articles, such as bottles, containers, and the like, many individual articles and parts are made that are not of the first quality, or that are not otherwise marketable. It is desirable to reuse (for example, recycle) the resin in these "out of grade" items. The resin from which the off-grade materials are made can be mixed with the virgin PET resin to recover the formation of other articles. In one embodiment, these articles are ground, pitted, or otherwise reduced to smaller parts (e.g., particles), for the purpose of preparing the resin for reuse. The particulate material obtained in this way is commonly referred to as "re-grinding". The re-grinding can be introduced into the virgin resin stream. The amount of regrind that may be present in the resin used to manufacture articles, such as preforms for bottles and / or blow molding containers, can vary over a wide range, depending on the availability of the resin, the final purpose of the article formed, and other different factors. The re-grinding may constitute from 0 to 100 percent of the resin used to form a processed article (e.g., injection molded), such as a preform, which can be used to blow-mold a container. For example, thermoforming may include re-grinding in an amount of about 40 to 100 times percent, and custom containers include re-grinding from about 0 to 30 percent, and containers for CSD / beer include re-grinding from about 0 to 15 percent, where the percentage is the percentage in weight, based on the amount of re-grinding and the total weight of the resin. Re-grinding amounts that vary from the above amounts may be present including any interval or sub-range of the above ranges, including any increase of 1, 2, 3, 5, and 10 percent. In a preferred embodiment of the invention, the solid shaped article formed from the polyester resin is a bottle preform. An example of a bottle preform is shown as Figure 5. Typically, the bottle preform consists of the polyester resin, but in other embodiments, the bottle preform may include additives, or it may be a mixture of the polyester with one or more different resins. Preferably, the bottle preform is made from the polyester resin by injection molding. The bottle preform can be any size, including the range from 12 or less grams to 300 or more grams for each preform. For example, the preforms from which the individual water bottles are blow molded can weigh from 12 grams or less to as much as 40 grams or more. Some preforms that are designed for CSD / beer applications can be as low as 20 grams or less, and as high as 65 grams or more. Other preform designs that can be used in custom container markets can be as low as 12 grams or less, or as high as 100 grams or more, and some preforms designed for use in the bottled water market , can be as low as 50 grams or less, or as high as 300 grams or more. Preferably, the bottle preform is made from the polyester resin by injection molding; however, other means are available for the manufacture of the preform, for example, compression molding. The bottle preform is cooled after injection molding, and can be stored for 6 months or less, up to 12 months or more, depending on storage conditions. Preferably, the injection molding that is carried out to form the bottle preform uses a multi-cavity mold. For example, an injection molding apparatus having multiple cavities is preferably used. Each cavity of the multi-cavity mold is capable of forming a single bottle preform. The removal and / or reduction of the change in the intrinsic viscosity of the polyester resin can be especially pronounced in injection molding processes using a mold having a high number of cavities. In these injection molding processes, a larger amount of the molten polyester resin must be pressurized into the multi-cavity mold, in comparison with a mold that has fewer cavities, because a larger volume of polyester resin must be used to form a greater number of bottle preforms. Accordingly, in one embodiment of the invention, an amount of molten polyester resin can be maintained at a temperature higher than the melting temperature of the polyester resin, for a longer period of time at a higher temperature, in comparison with conventional polyester resins and / or molding processes using conventional polyester resins. In the method of the invention, the lowest degree of intrinsic viscosity reduction is observed in the resin after melting and a prolonged heat history, as compared to polyester resins and / or conventional molding operations. The injection molding of the polyester resin to form a bottle preform can be carried out under different conditions. In a preferable way, injection molding is carried out with an injection molding apparatus that is capable of completely melting the polyester resin, and having sufficient injection pressure to fill a multi-cavity mold. The pressure of the extruder of this injection molding apparatus may contain a plurality of heating zones. The temperature of each heating zone is controlled in an independent manner. The number of heating zones is not limited, and preferably, the number of heating zones is four or more, more preferably five or more, of a most preferable of six or more, more preferably seven, more preferably eight or more, still more preferably nine or more, and most preferably 10 or more. Each heating zone is capable of heating the polyester resin to a temperature higher than the melting temperature of the polyester resin. The temperature of any zone can vary, for example, from 450 ° F to 650 ° F (from 232 ° C to 343 ° C), preferably from 475 ° F to 525 ° F (from 246 ° C to 273 ° C) , more preferably from 500 ° F to 575 ° F (from 260 ° C to 301 ° C), and most preferably from about 550 ° F (287 ° C). Any of the aforementioned temperatures can be varied by any increase, for example, of 2, 4, 6,8, or 10 ° F (of 1, 2, 3, 4, or 5 ° C), or any multiple of the same. The screw speed of an injection molding apparatus used to carry out injection molding can be varied as necessary to adjust the cycle time and other factors of the injection molding process. For example, the screw speed can be from 20 to 200 revolutions per minute, preferably from 30 to 160 revolutions per minute, more preferably from 40 to 120 revolutions per minute, more preferably from 50 to 80 revolutions per minute, and most preferably about 60 revolutions per minute. The screw speed can be varied in any increment of 1, 2, 4, 6, 8, and 10 revolutions per minute within any of the aforementioned ranges, or any multiple of the same. The back pressure of the injection molding process can be varied and can be in the range of 0 to 700 psig (from 0 to 49 kg / cm2), from 300 to 350 psi (from 21 to 24.5 kg / cm2), more preferably from 250 to 400 psi (from 17.5 to 28 kg / cm2), and especially preferably from 200 to 600 psi (from 14 to 42 kg / cm2). The cycle time of preference is less than 1 minute, more preferably less than 45 minutes, and most preferably less than 30 seconds. The time of the clamping opening cycle up to clamping opening. The cycle time is usually defined by the following functions: mold filling, partial cooling, mold opening, partial ejection, partial removal, mold closure. Simultaneously and within the same amount of time, the resin is melting in the liquefied state, the resin is undergoing conditioning (e.g., extrusion), and the molten resin (e.g., polymer melt) is in preparation to transfer to the space of the mold. One method includes feeding the resin to an extruder for melting, and mixing within a heated extruder with a revolving screw that compresses and conditions the polymer as it changes phase from a solid state to a liquid state; The liquefied resin is then transferred to a controlled volume that is transferred to a mold. Because these actions can coincide in a dependent manner, a correlation can be drawn between the time of the cycle and the time when the polymer It is in the liquid phase. This correlation may differ from part of bottle preform to part of bottle preform, and from mold to mold, and from machine to machine. During injection molding to form a bottle preform, or during blow molding an article configured from a bottle preform, to form a shaped article, such as a carbonated soft drink container, some degree of shrinkage of the bottle may occur. mold. The shrinkage of the mold is the amount of shrinkage associated with the article configured after the cooling and expulsion from the mold is completed. The shrinkage of the mold is a value that compares the dimensions of the finished and cooled shaped article with the values of the dimensions of the mold from which the shaped article was obtained. The values of mold shrinkage are an important feature of the configured articles, both of the bottle preforms and of the blow molded shaped articles, especially as regards the sealing, capping, and filtration characteristics of a sealed container prepared by the injection molding of a bottle preform, and subsequently the blow molding of the sealed container. If there is a substantial mold shrinkage, the seal between a lid and the liquid contained in the container may not be sufficient to prevent leakage and / or to otherwise prevent a seal seal from the container. In the method of the invention, the shrinkage value of the mold of the preform obtained by injection molding the resin of the invention, preferably does not change by an amount greater than the shrinkage value of the mold associated with the conventional polyester resin. Moreover, the shrinkage properties of the mold of the blow molded article obtained from the bottle preform are essentially equivalent or exactly the same as the shrinkage value of the mold for a blow molded article derived from a preform of bottle made of a conventional polyester resin. Preferably, the shrinkage of the mold is the same as the shrinkage of the mold for the corresponding conventional resins. The injection molded bottle preform can be used in a blow molding process to form an expanded bottle (e.g., a bottle or blow molded container). An expanded bottle formed from a preform obtained from the method of one embodiment of the invention is shown as Figure 6. During blow molding, the bottle preform is heated, for example, by infrared light, and subsequently expanded under pressure by means of a gas, or is initiated by mechanical means. The polyester resin can undergo a significant stretch during blow molding. For example, an axial stretch ratio in a blow molded bottle obtained from a preform can be from 1.5 to 3.5 times, preferably from 1.75 to 3.25 times, more preferably from 2 to 3 times, still more preferably from 2.25 to 2.7 times, and most preferably from about 2.5 times. The jump stretch ratio of the blow molded bottle can be, for example, 3 to 7 times, preferably 3.5 to 6.5 times, more preferably 4 to 6 times, more preferably about 4.5 to about 5.5 times, and still most preferably about 5 times. Typically, the bottle preform is blow molded in a straight-walled mold. However, other molds may be used, such as shaped and / or textured molds, and of all sizes, without restriction. One bottle shape is a 2 liter carbonated soft drink bottle. The formation of the expanded preform by blow molding can include heating the bottle preform with a plurality of lamps that provide infrared heat to the bottle preform. The preform can be heated to a temperature, for example, from 80 ° C to 150 ° C, preferably from 85 ° C to 140 ° C, more preferably from 90 ° C to 130 ° C, still more preferably from 95 ° C to 120 ° C, and most preferably about 100 ° C. Gas can be injected into the heated bottle preform to stretch the polyester resin at a stretch speed of 0.2 to 2.0 meters / second, preferably from 0.4 to 1.5, more preferably 0.6 to 1.2, and most preferably from 0.6 to 1.2. approximately 0.8 meters / second. The preform of The heated bottle can be inflated in the bottle mold with an initial pressure of about 20 bar, for example from 5 to 30 bar, more preferably from 8 to 22 bar. A final blow can be carried out with a gas pressure of 40 bar or more. The final blow can be used to better define the shape and / or texture of the container. In one embodiment, the temperature of the mold is colder than the temperature of the polyester bottle preform, and is preferably from 0 ° C to 100 ° C, more preferably from 10 ° C to 80 ° C, in a further manner. preferable from 15 ° C to 60 ° C, and most preferably from 20 ° C to 50 ° C. In a heat setting mode, the temperature of the mold is as high as 200 ° C, preferably 100 ° C to 200 ° C, more preferably 125 ° C to 175 ° C, and most preferably from 100 ° C to 200 ° C. 140 ° C to 160 ° C. The bottle, for example a bottle for carbonated or beer soda, formed from the polyester bottle preform, preferably it is free of nebulosity and pearlescence. The temperature of the bottle preform during blow molding can be adjusted in such a way that no pearlescence is observed in the blow molded article obtained from the bottle preform. A bottle preform temperature that is too low during blow molding can result in unacceptable pearlescence, while a temperature that is too high can result in haze. The gas barrier resistance of polyester resins used to make polyester-based bottles, by example, by blow molding, it can be improved by 100 percent or more, if the polyester resin is oriented. For carbon dioxide gas and oxygen gas, an oriented polyester bottle has a gas barrier strength of at least twice (2X) as large or greater than a non-oriented polyester bottle. The process of biaxial orientation provides the generation of lamellated crystals induced by tension. The oriented crystallites result in lower gas permeability and better mechanical properties. A biaxially oriented polyester bottle typically has a crystallinity of 20 to 30 percent (21 percent in the shoulder, 25 percent in the middle panel, 25 percent in the foot), which is based on the densities measured in a column of density gradient. Alternatively, a polyester resin can be modified with a co-barrier resin known to have a greater gas barrier resistance than PET. For example, polymers based on meta-xylene diamine (MXDA), such as MXD6, MXD6-IPA, MXD6-italic anhydride, etc., may have better gas barrier properties than PET. These polymers containing MXDA may also have a better gas resistance than certain nylons, such as nylon 6, nylon 6/6, etc. MXD6 is a semi-crystalline polyamide resin that can be produced by the poly-condensation of MXDA with adipic acid. The processes for producing these polymers containing MXDA are described, for example, in U.S. Patent Nos. 4,433,136 and 4,438,257, each of which is incorporated herein by reference in its entirety. In another aspect of the invention, the polyester resin obtained without solid phase polymerization is made by processing directly from a terminator (e.g., a thin or cleaned film evaporator), through a die, and subsequently granulate with or without cooling with water. In one embodiment, the resulting resin is extruded in the form of strands that can be cut at temperatures higher than the glass transition temperature of the resin. Preferably, the strands are cut at temperatures that are 10 ° C, 15 ° C, 20 ° C, 30 ° C, 40 ° C, 50 ° C or 100 ° C higher than the glass transition temperature of the resin, in a concurrent manner or after the strands have passed through a water bath. The fragments of preference are separated from the water as quickly as possible. The temperature on the outside of the granules may be lower than the temperature inside the granules. The fragments and / or granules can continue to crystallize by means of their internal residual heat (for example, crystallization of latent heat). The polymer (e.g., resin) used in the invention can be crystallized by latent heat, or alternatively, it can be crystallized in a conventional manner. Optionally, a fragment vibrator or a fluidized bed can be used to prevent the fragments from adhering to each other during heating and / or crystallization.

One way to reduce the tendency of the fragments to adhere to each other is by imparting a faster and more robust crystallinity to the fragments and / or granules formed during cooling and / or cutting. This may be especially the case if the resin contains more than one type of polymer. Some polyester-containing resins, such as resins containing an MXDA co-resin, may be more susceptible to adhesion or lumping when heated (eg, when heated above the glass transition temperature, or near the glass transition temperature). Preferably, these resins and / or resin mixtures are not cooled below the Tg following the extrusion (for example, when forming strands), so that the crystallization of latent heat may take place. The granules and / or fragments thus formed are less susceptible to adhesion, even when subjected to polymerization in the solid state. In a preferred embodiment of the invention, the resin that is processed in the process of the invention is a polyester resin that has been subjected to crystallization of the latent heat. The resin compositions can also be cooled / crystallized in a manner that provides an amorphous fragment and / or granule. Cooling with or without cutting may provide fragments and / or granules that are amorphous. As the melt polymerization reaches an intrinsic target viscosity, the molten polyester is pumped (by example, PET, PEN, etc.) in the melted state, through a die. The resin can be granulated using any conventional method, including any of the methods described below. In conventional melt poly-condensation processes for the preparation of polyester compositions, such as PET compositions, or compositions containing PET, the molten polyester is completely quenched as transparent / amorphous particles. In one embodiment of the invention, the resulting resin (for example, after passing the molten resin through a die) can be treated by any conventional method. For example, dry / cold granulation can be carried out, by which the transparent / amorphous fused resin is rapidly quenched in a water bath. The water in the quenched resin is blown first, and then the resin is granulated. In another embodiment of the invention, wet / cold granulation can be used. A wet / cold granulation process can use a granulator partially under water. The rapid shutdown process can be carried out by continuously spraying the molten strands that fall from the resin, with cold water. The wet / cold threads are then granulated by a rotary cutter, which may be partially in the water. The granulation under water can also be used to form the granules and / or fragments of the resin. For example, granulation under conventional water of the resin strands can be used to form the granules and / or fragments of the resin. The Granulation under water can take place with a granulator on the face of the die. Preferably, a die-face granulator is used under water to obtain a solid form of the resin, which is crystallized by the latent heat. In another embodiment of the invention, wet / hot granulation can be used. As the molten resin emerges from the holes in a die, it can be cut immediately while it is hot. The hot cutting preferably takes place above the glass transition temperature or the melting temperature of the resin, and typically provides spheroidal and / or ellipsoidal particles. In a preferred embodiment of the invention, the molten polyester composition is partially cooled to solidify the composition. The temperature at which the polyester compositions are partially cooled is between the glass transition temperature (Tg) and the melting point of the polyester resins. The polymer composition is then maintained at a temperature of 170 ° C + 50 ° C, preferably + 40 ° C, and more preferably + 30 ° C, especially preferably + 20 ° C, for the crystallization of the PET, by separating the hot fragments from the water as quickly as possible. The separation of the solidified polyester composition, for example, from a water bath, can be facilitated with a centrifugal dryer, a vibrating plate, and / or a vibrating screen, such as those available from Rieter, BKG, and Gala Industries. The residual heat of The fragments can be used for in situ crystallization without a conventional crystallizer. Preferably, this aspect of the invention is carried out on a polyester resin. The polyester resin can be made by a melt-phase reaction carried out in a plurality of reactors connected in series, in parallel, or both in series and in parallel. The reaction of the dicarboxylic acid monomer and diol can be carried out in the absence of any solvent (for example, a diluent component that does not form a substantial portion of the polymeric units that react in the resin composition). The monomer units are reacted to form a material having an intrinsic viscosity which may be in the range, preferably, in an embodiment of the invention, from 0.2 to 0.5 of intrinsic viscosity for the final terminator. The molten material thus formed in the melt phase reactor is then pumped or transferred to a finishing reactor. The finishing reactor may be a reactor such as a cleaned or thin film reactor, which provides substantial contact between the surface areas of the reactor, and which results in a high mixing of the molten reacted melt product. The terminator can be carried out in one or more reactors connected in series, in parallel, or both in series and in parallel. In addition to the cleaned film reactor, one or more tube reactors may be included. The resin product obtained from the last finishing reactor may have an intrinsic viscosity of 0. 7 to 0.9, preferably from about 0.75 to 0.85, and most preferably about 0.80, for example, for a resin for CSD / beer. The molten resin product obtained from the finishing reactor is then preferably subjected to a polymer filtration in the molten form. The polymer filtration can be carried out in one or more steps. For example, after the resin material is filtered from the last finishing reactor, one or more co-barrier resins can be mixed with the filtered and melted polyester resin composition. In one embodiment of the invention, a co-barrier resin is extruded by melting, and then mixed with the molten polyester resin composition, which is filtered, and in a molten form. The mixed streams obtained from the molten co-barrier resin and the filtered polyester resin composition can be directed to a static mixer for mixing. After mixing, preferably continuous mixing, the mixed and melted material is directed towards a granulator to solidify the mixed polyester resin composition. For example, the mixed polyester resin composition can be pumped through a die containing a series of holes. The molten material that comes out of the holes is granulated. As the resin enters the water of the granulator under water, it solidifies slowly. The water of the granulator under water can be maintained at a high temperature. Preferably, the water of the granulator under water it is maintained at a temperature greater than 50 ° C, preferably greater than 80 ° C, still more preferably greater than 90 ° C. Preferably, the hot water of the granulator below the water is maintained at a temperature that is above the glass transition temperature of the polyester resin composition, and below the melting point of the polyester resin composition. In another embodiment of the invention, to avoid crystallization of the latent heat, the water temperature is preferably below 80 ° C, preferably below 60 ° C, and most preferably below 50 ° C. In carrying out the solidification of the mixed polyester resin composition melted with hot water, and when cutting, the process of one embodiment of the invention provides granules and / or fragments of solid polyester resin composition which is in the crystalline phase . Because the granules and / or fragments are in the crystalline phase, they may appear opaque. The resultant solid, opaque, crystalline polyester resin composition can then be transferred to a product silo for intermediate storage or packaging. The product thus obtained can be mixed with the co-barrier resin in solid form, for example, in a granule or powder, to form a mixture of granules and / or fragments of the polyester resin composition of the invention, and a co-barrier resin in solid form. Then the resulting composition can be used for injection molding operations, including the formation of preforms for blow molded articles, such as containers and bottles. One embodiment of the invention includes a polyester resin obtained by the reaction of monomeric units of a diol and dicarboxylic acid, to form a polyester having the reactive monomer units present in an equimolar or quasi-equimolar amount. In a preferred embodiment, the diol and the dicarboxylic acid are reacted to form a polymer having the monomeric units present in approximately equimolar amounts. The diol and the dicarboxylic acid can be reacted in amounts that are not exactly in an equimolar amount. For example, the diol may be present in greater amounts than the dicarboxylic acid. During the poly-condensation reaction, excess diol is typically removed with heat at reduced pressure. Suitable polyesters useful in the compositions of the invention are well known in the art, and are formed in general from repeating units comprising one or more carboxylic acid components selected from terephthalic acid (TPA), isophthalic acid, naphthalene dicarboxylic acid, 2,6-naphthalene dicarboxylate dimethyl or (NDC) ), hydrolyzed 2,6-naphthalene dicarboxylic acid (HNDA), and one or more diol components selected from ethylene glycol, diethylene glycol. 1,4-cyclohexane-dimethanol, 1,3-propanediol, 1,4-butanediol, propylene glycol (1,2-propanediol), 2-methyl-, 3-propanediol, and 2,2-dimethyl-1,3-propanediol (neopentyl) -glycol), and mixtures of same. Preferred polyesters of the present invention include poly (ethylene terephthalate) (PET), poly (ethylene naphthalate) (PEN), poly (polyethylene isophthalate) (PEI), and poly- (trimethylene terephthalate) (PTT) ), po I i - (trimethylene naphthalate) (PTN), and most preferably poly- (ethylene terephthalate) (PET). The polyesters of one aspect of the invention can be made using processes well known to those skilled in the art. Suitable polyesters can be produced in a conventional manner, by reacting a dicarboxylic acid having from 2 to 40 carbon atoms, with one or more polyhydric alcohols, such as glycols, diols, or polyols, containing from 2 to about 20 carbon atoms, preferably from 6 to 12 carbon atoms. The general conditions that produce polyesters, including the process conditions, the catalysts, and the additives, are known to the experts. Methods for producing polyester materials and combinations of polyesters with other polymeric materials are given in W, R, Sorenson and TW Campbell, "Preparative Methods of Polymer Chemistry," (Interscience Publishers, New York 1968, and the following editions), and the "Encyclopedia of Polymer Science and Engineering", 2nd Edition, HF Mark et al. (John Wiley &Sons, New York 1985), in particular Volume 12, pages 1-290 (polyesters in general), and especially pages 259-274 for the resin manufacturing processes, each of which is incorporated herein by reference.

The dicarboxylic acid which can be used to make the polyester-containing compositions of the invention include alkyl dicarboxylic acids having from 2 to 20 carbon atoms, preferably from 6 to 12 carbon atoms, and an aryl-dicarboxylic acid substituted by aryl or alkyl containing from 8 to 24 carbon atoms, preferably from 8 to 16 carbon atoms. Additionally, diesters of alkyl dicarboxylic acids having from 4 to 20 carbon atoms, or diesters of aryl-dicarboxylic acids substituted by alkyl having from 10 to 20 carbon atoms can be used. The dicarboxylic acid component of the polyester of the invention can be optionally modified with up to about 30 mole percent, preferably up to about 25 mole percent, more preferably up to about 20 mole percent of one or more different dicarboxylic acids. In another embodiment of the invention, the polyester is modified with less than 10 mole percent, preferably less than 8 mole percent, more preferably 3 to 6 mole percent of one or more different dicarboxylic acids. These additional dicarboxylic acids include aromatic dicarboxylic acids preferably having from 8 to 14 carbon atoms, aliphatic dicarboxylic acids preferably having from 4 to 12 carbon atoms, or cycloaliphatic dicarboxylic acids preferably having from 8 to 12 carbon atoms. . Examples of the dicarboxylic acids that must be included with the Terephthalic acid in the resin compositions of the invention in major or minor proportions include: italic acid, isophthalic acid, 5- (sodium-sulfo) -isophthalic acid (5-Na + S03"IPA) and 5- (lithium-sulfo) acid ) -isophthalic (5-Li + S03"-IPA), naphthalene-2,6-dicarboxylic (and also the isomers 1,4, 1,5, 2,7, and 1,2, 1,3, 1,6, 1,7 , 1,8, 2,3, 2,4, 2,5, 2,8), cyclohexane-dicarboxylic acid, cyclohexanediacetic acid, diphenyl-4,4'-dicarboxylic acid, succinic acid, glutaric acid, adipic acid, acid azelaic, sebacic acid, bibenzoic acid, hexahydrophthalic acid, bis-p-carboxy-phenoxy-ethane, and mixtures thereof, and the like. Preferred dicarboxylic acids include isophthalic, terephthalic, and naphthalene dicarboxylic acids. In a preferred embodiment of the invention, the polyester matrix resin comprises from 5 to 30 mole percent isophthalic acid, and from 1 to 15 mole percent of a naphthalene dicarboxylic acid, more preferably from 2 to 10 mole percent of the naphthalene dicarboxylic acid, and still more preferably from 3 to 6 mole percent of the naphthalene dicarboxylic acid, in the form of the monomeric units that react. Terephthalate polyesters for transparent container applications are typically made from a terephthalic acid and ethylene glycol, or from a terephthalic acid and 1,4-cyclohexanediol. Suitable dicarboxylic acids include terephthalic acid, isophthalic acid, malonic, succinic, glutaric, adipic, suberic, sebacic, maleic, and fumaric acid, all of which are well-known dicarboxylic acids, or mixtures thereof, in such a way that a copolyester is produced. Preferred are glycols or polyhydric diols containing from 2 to 8 carbon atoms, more preferably ethylene glycol. The glycol ethers or diol ethers having from 4 to 12 carbon atoms can replace the glycol or diol. Suitable glycols, in addition to ethylene glycol and 1,4-cyclohexanedimethanol (CHDM), include diethyl glycol, propylene glycol (1,2-propanediol), 1,3-propanediol, 2-methyl-1,3-propanediol, 2,2-dimethyl-1,3-propanediol (neopentyl glycol), 1,2-butanediol, 1,4-butanediol, pentaerythritol, glycols and similar diols, and mixtures thereof. These compounds and the processes for making the polyesters and co-polyesters using the compounds are well known in the art. In addition, the glycol component can be optionally modified with up to about 15 mole percent, preferably up to about 10 mole percent, more preferably up to about 5 mole percent of one or more diols other than ethylene glycol. These additional diols include cycloaliphatic diols preferably having from 6 to 20 carbon atoms, or aliphatic diols preferably having from 3 to 20 carbon atoms. Examples of these diols include: diethylene glycol, triethyl glycol, propylene glycol, 1,4-cyclohexane-dimethanol, propane-1,3-diol, butane-1,4-diol, pentane-1,5-diol, hexane-1, 6- diol, hexane-1,4-diol, 1,4-cyclohexanedimethanol, 3- methyl-pentanediol- (2,4), 2-methyl-pentanediol- (, 4), 2,2,4-trimethyl-pentanediol - (1, 3), 2-ethyl-hexanediol- (1, 3), 2,2-diethyl-propanediol- (1, 3), hexanediol- (1, 3), 1,4- di- (hydroxy-ethoxy) -benzene, 2,2-bis- (4-hydroxy-cyclohexyl) -propane, 2,4-dihydroxy-1,1,3-tetramethyl-cyclobutane, 2, 2-bis- (3-hydroxy-ethoxy-phenyl) -p-clothes, neopentyl-glycol, 2,2-bis- (4-hydroxy-propoxy-phenyl) -propane, mixtures thereof, and the like. The polyesters can be prepared from two or more of the above diols. The polyester may also contain small amounts of trifunctional or tetrafunctional comonomers, such as trimellitic anhydride, trimethylolpropane, pyromellitic dianhydride, pentaerythritol, and other polyester-forming polyols or polyols generally known in the art. The polyester resins described herein may generally contain one or more other elements or components conventionally used in the manufacture of polyester resins. For example, a typical resin may contain elements such as Co, Ti, Sb, and / or P, which may be present in the resin compositions due to their use and / or presence in the catalysts, heat stabilizers, and colorants used. during the polymerization and / or processing of the polyester resins. For example, Sb, Ge, Ti, or Sn can be used for the melt polymerization, for example, in the form of organic titanates dibutyltin dilaurate, tin organics, germanium dioxide, antimony trioxide (Sb203), antimony triacetate, and / or antimony glycolate (Sb2 (gly) 3), or oxides of the respective metals (eg, Ti02, Ge02, etc.). There may be phosphorus present as a residue of any trialkyl phosphate or phosphite present during the polymerization and / or processing of the resulting resins. The elements that are present as residues of the coloring agents used, for example, to modify and / or control the yellowing index, such as Co (OAc) 2, may also be present. Typically, the materials that are present as residues of the polymerization catalysts or processing additives are present in an amount of 1 to 1,000 parts per million, preferably 5 to 500 parts per million. Also, although not required, other additives normally used in polyesters and / or other thermal plastic compositions may be present in the resin compositions of the invention. These additives can include, but are not limited to, dyes, matizers, carbon black pigments, glass fibers, fillers, impact modifiers, antioxidants, stabilizers, flame retardants, reheating aids, acetaldehyde reducing compounds, oxygen scavengers, enhancement aids of barrier, and mixtures thereof. There may also be anti-blocking agents present, along with other lubricants. The process for forming the polymer compositions of the invention in a manner that excludes solid state polymerization includes the methods described in published Patent Applications of the United States of America Nos. 2005/0029712 and 2005/0161863; and in the Patents of the United States of North America Nos. 5,980,797; 5,968,429; 5,945,460; Y 5,656,719 (each of which is incorporated herein by reference in its entirety). In some of the embodiments described herein, which include polyester compositions that are defined by their physical and chemical properties, such as intrinsic viscosity, crystallinity, clarity, etc., conventional processes, such as the process described, may be employed. in Figure 1, to form the polyester or the co-polyamide. The molten polymeric material can be mixed with one or more different molten polymer streams containing polymeric polyester material made from the same monomer units or from different monomer units, to form a blend of molten polymeric material (e.g. polyester materials). In a preferred embodiment, the resulting polymer composition is mixed with one or more additives, while they are melted, and then used in the formation of the preform articles. The intrinsic viscosity of the matrix resin (e.g., the polyester matrix resin) may be lower in the preform than the intrinsic viscosity of the resin from which the preform is molded. This can happen for a number of reasons. For example, the addition of a co-barrier resin having a different intrinsic viscosity may affect, for example, raising or reducing, the intrinsic viscosity of the final composition, which may be a mixture of the matrix resin and the resin of co-barrier. In addition, after a processing step to prepare a preform, it is possible that the history of heat incurred in this manner may result in a decomposition or depolymerization of the matrix resin, thereby lowering the intrinsic viscosity. For the polyester matrix resin, the polymerization of the monomer units is preferably carried out to provide an intrinsic target viscosity of 0.7 to 0.95, preferably 0.75 to 0.85, and most preferably the intrinsic viscosity is about 0.80 deciliters. gram, for example, for a bottle for CSD / beer, or 0.72, for example, for a bottle for water. The concentration of acetaldehyde in the polyester resins is an important property of the resins, and can determine whether a particular resin is suitable, for example, for a contact application with food or with water. During the processing of conventional polyester resins, the decomposition of the resin during processing (for example, as it accompanies a change, such as a loss in intrinsic viscosity) can lead to the formation of acetaldehyde. In one embodiment of the present invention, a process that includes the processing of a polyester resin is carried out with a relatively lower rate of increase in the concentration of acetaldehyde relative to the concentration of acetaldehyde in the polyester resin before the processing, such as subjecting the polyester resin to a heat history that includes melting and solidifying the resin polyester. In one embodiment of the invention, the amount of acetaldehyde formed during the processing of the resin made without polymerization, in the solid state, may be less than the amount of acetaldehyde formed during the processing of a conventional resin made with a process including polymerization in solid state. Preferably, during the processing of a resin made without solid state polymerization, the amount of acetaldehyde formed during processing is not greater than the amount of acetaldehyde formed during the processing of a conventional resin made with a process including solid state polymerization. . More preferably, the amount of acetaldehyde formed during the processing of the invention is at least 5 percent less than the amount of acetaldehyde formed during the processing of a conventional resin., more preferably at least 10 percent less, even more preferably at least 15 percent less, more preferably at least 20 percent, still more preferably at least 25 percent less, and especially preferably at least 30 percent less than the amount of acetaldehyde formed in the conventional resin, and more preferably at least 50 percent less than the amount of acetaldehyde formed during the processing of a conventional polyester resin. The amount of reduction in acetaldehyde is calculated by measuring acetaldehyde before and after the melting and processing of the invention, and determining the change in the acetaldehyde formed in relation to the amount of acetaldehyde formed in the conventional resin. During the normal processing of polyester resins (for example, during the melting and processing of conventional resins), it is not uncommon for the concentration of acetaldehyde in the polymer (for example, the molded article) to be 300 percent by weight. 1,000 percent greater than the amount of acetaldehyde present in the resin, for example, in the granules and / or fragments, before processing (eg, before melting and infusion molding to form a preform). In the invention, the amount of acetaldehyde is likely to increase in the resin after processing in the absence of acetaldehyde scavengers or reducing agents. However, the increase in the concentration of acetaldehyde observed in the invention may be less than the increase in the acetaldehyde concentration observed when conventional polyester resins made by solid state polymerization are melted and / or processed. In one embodiment, the concentration of acetaldehyde in a molded article of the invention increases by no more than 500 percent after melting and processing (eg, conventional injection molding of the resin to form a bottle preform), preference for no more than 300 percent, preferably no more than 250 percent, still more preferably no more than 225 percent, still further preferably no more 200 percent, especially preferably no more than 175 percent, still more preferably no more than 150 percent, and especially preferably no more than 100 percent. In other embodiments, the increase in the amount of acetaldehyde observed for the virgin resin compared to the virgin resin after processing (e.g., injection molding) is not greater than a 100 percent increase in acetaldehyde. In a further embodiment of the invention, the polymeric compositions of the invention contain one or more additives, such as fillers. The fillers may include materials such as clay, nanomaterials, and / or other polymeric materials, for example nylon.

The polyester compositions of the invention preferably contain a PET resin containing copolymerized IPA monomer units. The invention encompasses at least one PET resin low in IPA and a PET resin high in IPA. For example, a composition low in IPA (i) that contains a PET resin having an amount of IPA monomer units of up to 6 molar percent. In a preferred embodiment, the PET resin low in IPA contains up to 5 mole percent of IPA monomer units. More preferably, the PET resin low in IPA contains from 2 to 4 mole percent of polymerized IPA monomer units, based on the total number of moles of monomeric dicarboxylic acid units. Subsequently in the present, the PET resin containing a low amount of IPA monomer units are referred to as the PET resin low in IPA. Another PET resin is a PET resin high in IPA, for example (ii) the PET resin high in IPA, wherein the IPA monomer units are present in an amount of 6 to 30 molar percent, preferably 8%. at 25 percent, more preferably from 9 to 20 percent, and most preferably from about 10 to 15 percent per mole, based on the total number of moles of dicarboxylic acid in the PET polymer. Other intervals include 10 to 28 percent, 12 to 30 percent, and all intervals and sub-intervals that appear between and either 14 percent, 16 percent, 18 percent, 20 percent, 22 percent , 24 percent, and 26 percent, and / or the aforementioned ranges. Therefore, in the preferred embodiments, the polyether compositions of the invention may include a PET matrix resin, such as a low IPA resin, or the high IPA resin described above, together with one or more additives, such as a filler inorganic, or a co-barrier resin. Preferably, a composition comprising the low IPA resin contains from 2 to 8 weight percent of a co-barrier resin, wherein the weight percentage is based on the total weight of the composition. More preferably, the co-barrier resin is present in the PET matrix resin low in IPA in an amount of 3 to 6 weight percent, and still more preferably, the co-barrier resin is present in an amount of 4 to 5 weight percent. In another preferred embodiment, the PET composition of the invention contains the high IPA resin as a matrix, and a co-barrier resin. The co-barrier resin is preferably present in the matrix of the PET resin high in IPA in an amount of up to 2.5 weight percent, preferably less than 1.5 weight percent, more preferably up to 0.5 weight percent. percent by weight, where the percentage by weight is based on the total weight of the composition. In a preferred embodiment, the polymeric polyester composition contains a solid clay filler and / or a nanomaterial. The clay filling is preferably in the form of an expanded clay or expanded mica. Examples of the expanded clays and / or micas include organo-clays. Some organo-clay materials are preferred. Organo-clays, such as CLOISITE 93 A, CLOISITE 30B, and other CLOISITE products from Southern Clay Products, Gonzalez, TX, show excellent sputtering in an MXD6 resin matrix (6001 or 6007). The dosage of the organoclays 30B or 93A may be about 5 weight percent. Other ranges in which the filling may be present include from 1 to 10 weight percent, from 2 to 8 weight percent, and from 3 to 6 weight percent. Preferably, the organoclay is present in a matrix containing a clay containing MXD6, and the organoclay it is present in an amount of about 5 percent relative to the total MXD6 resins. The filler may be present in other amounts, such as from 1 to 20 weight percent, from 2 to 15 weight percent, from 3 to 10 weight percent, and from 6 to 8 weight percent. Mixtures of the organoclay can be melt-mixed with an amine-containing resin, with the PET resin compositions, to obtain a composition comprising a matrix resin, an organoclay filler, and a co-barrier resin. This is a promising approach for the nano-platelets to be indirectly dispersed in a polyester resin matrix. Preferably, the organoclay and / or nanomaterial materials are magnesium aluminum silicate plates layered on an organically modified nanometer scale. Typically, organo-modified organoclasts are derived from platelets that are approximately 1 nanometer thick, and from 70 to 150 nanometers crosswise. The process of organic modification of platelets includes contacting platelets with organic chemicals, such as quaternary ammonium salts. For example, clays in nanoparticles in contact with quaternary ammonium salts, such as the salt of quaternary ammonium hydrogenated tallow with dimethylbenzyl (2MBHT), the tallow quaternary ammonium salt of methyl-bis- (2-hydroxy) -ethyl) (MT2EtOH), and methyl dihydrogenase tallow ammonium (M2HT), are preferred. The sizes of particles may be about 6 microns, but any size that allows homogeneous inclusion of the particles in the matrix and / or the co-barrier resin can be used. In a preferred embodiment, the organoclay and / or the nanomaterial is first dispersed in a co-barrier resin, such as an MXDA-copolyamide, such as one containing IPA and terephthalic acid, together with an amount of ethylene glycol or other diol, and MXDA (meta-xylene-diamine). By first dispersing the inorganic filler, such as the organoclay filler, in the co-barrier resin (for example, in an MXDA-copolyamide resin), the inorganic filler can be better dispersed in the polyester matrix resin (by example, the PET matrix resin). The inorganic filler can be dispersed in the co-barrier resin in the solid state, by mixing the powders of the inorganic filler and the co-barrier resin. The powder mixture can then be mixed directly with the fused matrix resin, or it can be mixed with a molten resin after first melting the co-barrier resin mixture and the inorganic filler. In one embodiment, a master batch of inorganic co-barrier / filler is prepared. The inorganic filler is mixed with the molten co-barrier resin to form granules and / or strands of a masterbatch containing the co-barrier resin as a matrix resin, and, dispersed therein, the inorganic filler. The inorganic filler may be present in an amount of up to 25 weight percent, based on the total weight of the co-master batch. barrier / inorganic filler. Preferably, the inorganic filler is present in an amount of up to 20 percent, more preferably in an amount of up to 15 percent, in a further preferred embodiment, the inorganic filler is present in the master batch mixture. co-barrier / inorganic filler and / or resin, in an amount of up to 10 weight percent, and most preferably 1 to 5 weight percent. The inorganic filler may be present in an amount of 0.05 to 2.5 weight percent, based on the total weight of the composition. More preferably, the inorganic filler is present in an amount of 0.1 to 2.0 percent by weight, still more preferably 0.5 to 1.5 percent by weight, and most preferably, the inorganic filler is present in an amount about 1 weight percent. In another preferred embodiment, the polymeric polyester composition (e.g., the PET composition) is mixed with a polymeric filler, such as a polymer based on amide powder (e.g., nylon), or other thermoplastic materials. The resins of the invention (e.g., polyester resin compositions) may contain one or more polyamides or thermoplastics. Any polyamide can be present in the compositions of the invention, including, for example: poly- (m-xylene-adipamide), poly- (hexamethylene adipamide), polycaprolactam, poly- (hexamethylene-isophthalamide), and poly- (hexamethylene) -isophtalamide-co-terephthalamide). Polyamides that are copolymers, for example, of a polyester, they can also be present. Any polyamide / polyester copolymer may be present in the composition of the invention, including: polyamides including polymerized units of isophthalic acid, terephthalic acid, cyclohexanedicarboxylic acid, meta-xylen-diamine, para-xylene-diamine, 1, 3- or 1,4-cyclohexan- (bis) -methylene, one or more aliphatic acids with 6 to 12 carbon atoms, aliphatic amino acids with 6 to 12 carbon atoms, lactams with 6 to 12 carbon atoms, diamines if Attics with 4 to 12 carbon atoms. There can be polyamide dendrimers present, including polyamide dendrimers containing polymerized dicarboxylic acids. Preferred polyamides are poly- (m-xylylene-adipamide), poly- (hexamethylene-adipamide), polycaprolactam, poly- (hexamethylene-isophthalamide), poly- (hexamethylene-adipamide-co-isophthalamide), poly- (hexamethylene-adipamide) -co-terephthalamide). Especially preferred is MXD6, which is a polymer of meta-xylylene diamine and adipic acid. Copolymers of MXD6 with an italic acid are also preferred. Mixtures of MXD6 with one or more polyester resins, such as polyethylene terephthalate, and / or polyethylene terephthalate resins modified with meta-xylylene diamine. The polymeric filler may be present in amounts of 1 to 20 percent, of 2 to 18 percent, of 4 to 16 percent, of 5 to 15 percent, of 6 to 12 percent, of 8 to 11 percent, and any interval or sub-interval between the mentioned values, based on the total weight of the resins.

Preferred resin compositions of the invention include PET mixtures with at least one polyamide, such as MXD6, or an MXD6 polymer wherein up to 25 percent of the adipic acid monomer units are replaced with a dicarboxylic acid, such as isophthalic acid. Instead of the copolymer, a PET mixture can be used with a different polyester, such as ethylene poly naphthalate (PEN). Preferably, an organic filler may be present in an amount of up to 10 weight percent. More preferably, the organic filler is present in an amount of 1 to 8 weight percent. Still more preferably, the organic filler is present in an amount of 3 to 6 weight percent, based on the total weight of the composition. In a very preferable way, the organic filler is present in an amount of about 5 weight percent. In stretch blow molding, the PET chains can be aligned during biaxial orientation. The presence of nylon can produce an even closer chain alignment when compared to PET, due to the intermolecular strength of the hydrogen bond. For the bottle molded from conventional PET resins, a barrier improvement of about 40 percent can be observed if the temperature of the PET chains is reduced by 12 ° C from room temperature, for example, about 25 ° C. C. The decrease in the temperature of the PET chains also decreases their effective free volume.

Molecular orientation tends to increase the interfacial area of the mixture. The secondary link (interaction) between PET and MXD6 (or MXIPA) can be stronger to reduce the chain's mobility in this way, to reduce the effective free volume of the mixture. TEM is a good technique for taking two-dimensional micrographs (2-D) of the dispersion in a minor phase in a continuous phase. TEM is also useful to understand the effective dispersion (exfoliation or intercalation) of an organically modified nano-clay, in an organic polymeric matrix. For incompatible PET / MXD6 mixtures, MXD6 in a minor phase is usually stained with a 1 percent aqueous phosphotungstic acid (12 W03 · H3PO4 · H20), which marks the amine and end groups. If it is necessary to dye the PET, Ru04 steam must be used, which reacts with the acid ends. If the sample was not stained, the dark lines in the TEM image are the edges of the scattered organoclay platelets with high amplification. Platelet morphology or laminar morphology account for the substantial reduction of gas permeation rates in immiscible mixtures. The performance of the resin barrier bottles in monolayers depends, for example, on the base resins, the degree of crystallinity, the molecular orientation of the preforms by stretching, and the distribution of the material resulting from the bottles. PET preforms are usually designed to take advantage of the strong tightening effect to achieve a good distribution of the material. The intrinsic viscosity (IV) has a regularly strong effect on the tensile hardening behavior of PET. For CSD applications, preferably injection molded preforms can have an intrinsic viscosity of 0.70 to 0.95 to produce a normal stretch for good tensile hardening. EXAMPLES The intrinsic viscosity of the samples of a polyester resin composition was tested. The control groups included a polyester resin composition containing a conventional commercially available polyester resin made with a process that included solid state polymerization. The intrinsic viscosity of the polyester resin composition was measured on the virgin material before being subjected to fusion, other than the initial granulation process. A polyester resin composition containing only polyester resin made by a method that did not include solid state polymerization was compared to the conventional polyester resin. Except for the intrinsic viscosity, the resin produced by polymerization not in the solid state (eg, a resin according to the invention), was the same in its composition as the conventional commercially available polyester resin, except for the difference in the method of manufacture. The intrinsic viscosities before and after processing (ie, before and after injection molding) to form a bottle preform), are given in Tables 1 to 4. Fusion and Processing Conditions: The resins were dried prior to injection molding. The point of establishment of the dryer was 300 ° F (148 ° C), with a dew point of -25 ° F to -47 ° F (-31 ° C to -43 ° C). Drying was carried out for at least 6 hours before injection molding. The mold of the bottle preform was cooled with water, with a central supply at 50 ° F (10 ° C). The static temperature of the molten resin was 537 ° F to 563 ° F (280 ° C to 295 ° C), with a peak melting temperature of 572 ° F to 609 ° F (300 ° C to 320 ° C). The hydraulic injection pressure was from 1,175 to 1,750 psi (82.25 to 122.5 kg / cm2). The manifold setting temperatures (five in total) were 540 ° F (282 ° C). The firing temperatures of the container head and zone were 535 ° F to 555 ° F (279 ° C to 290 ° C). The extruder zones were from 535 ° F to 580 ° F (279 ° C to 304 ° C). Similar resins were processed under similar conditions. Following are examples of the profiles of the extruder: BHE-535 ° F (279 ° C); BH-535 ° F (279 ° C); E6-535 ° F (279 ° C); E5-540 ° F (282 ° C); E4-540 ° F (282 ° C); E3-545 ° F (285 ° C); E2-548 ° F (286 ° C); E1-550 ° F (287 ° C); BHE-540 ° F (282 ° C); BH-540 ° F (282 ° C); E6-542 ° F (283 ° C); E5-547 ° F (286 ° C); E4-547 ° F (286 ° C); E3-552 ° F (288 ° C); E2-555 ° F (290 ° C); E1-557 ° F (291 ° C); BHE-545 ° F (285 ° C); BH-545 ° F (285 ° C); E6-549 ° F (287 ° C); E5-554 ° F (290 ° C); E4-554 ° F (290 ° C); E3- 559 ° F (292 ° C); E2-562 ° F (294 ° C); E1-564 ° F (295 ° C); BHE-541 ° F (282 ° C); BH-546 ° F (286 ° C); E6-546 ° F (286 ° C); E5-546 ° F (286 ° C); E4-554 ° F (290 ° C); E3-556 ° F (291 ° C); E2-558 ° F (292 ° C); E1-560 ° F (293 ° C); BHE-548 ° F (286 ° C); BH-553 ° F (289 ° C); E6-556 ° F (291 ° C); E5-556 ° F (291 ° C); E4-561 ° F (294 ° C); E3-566 ° F (296 ° C); E2-568 ° F (297 ° C); E1-570 ° F (298 ° C); BHE-555 ° F (290 ° C); BH-560 ° F (293 ° C); E6-566 ° F (296 ° C); E5-566 ° F (296 ° C); E4-571 ° F (299 ° C); E3-576 ° F (302 ° C); E2-578 ° F (303 ° C); E1-580 ° F (304 ° C).

Table 1 SSP Degree of CSD / Beer Sample Shape IV Sample of pre-dryer: Box 1 Fragment NA 0.835 Sample of pre-dryer: Box 2 Fragment NA 0.837 Sample of pre-dryer: Box 3 Fragment NA 0.840 Post-dryer sample: A (566 ° F) (296 ° C) Fragment NA 0.829 Sample of post-dryer: B (571 ° F) (299 ° C) Fragment NA 0.823 Sample of post-dryer: C (576 ° F) (302 ° C) Fragment NA 0.826 Preform sample: A (566 ° F) (296 ° C) Preform 8 0.799 Preform 25 0.799 Sample Shape IV Preform sample: B (571 ° F) (299 ° C) Preform 8 0.797 Preform 25 0.797 Preform sample: C (576 ° F) (302 ° C) Preform 8 0.791 Preform 25 0.798 The resin made without polymerization in the solid state was subjected to the same drying and injection molding conditions as the conventional solid state polymerized resin. The measurements of the intrinsic viscosity are given in the following Table 2.

Table 2 No SSP Grade of CSD / Beer Sample Shape IV Sample of pre-dryer: Octabin 29 Fragment NA 0.801 Sample of pre-dryer: Octabin 30 Fragment NA 0.799 Post-dryer sample: D (565 ° F) (296 ° C) Fragment NA 0.804 Sample of post-dryer: E (570 ° F) (298 ° C) Fragment NA 0.810 Post-dryer sample: F (575 ° F) (301 ° C) Fragment NA 0.816 Sample Shape IV Preform sample: D (565 ° F) (296 ° C) Preform 8 0.792 Preform 25 0.790 Preform sample: E (570 ° F) (298 ° C) Preform 8 0.791 Preform 25 0.792 Preform sample: F (575 ° F) (301 ° C) Preform 8 0.799 Preform 25 0.798 As can be seen in Tables 1 and 2 above, the intrinsic viscosity of the resin made by a process including changes in solid state polymerization by approximately 0.04 deciliters / gram, compared to a resin made without solid state polymerization (by example, the resin of the invention), shows a reduction in the intrinsic viscosity of only about 0.015 deciliters / gram when the processing of both resins is carried out under the same conditions. A similar test was carried out on a polyester resin to be used in the formation of a bottle for water. The measurements of the intrinsic viscosity for the resin made with solid state polymerization were compared with the data for a resin made without solid state polymerization in the ig u i etes Tables 3 and 4, respectively. Tab l a 3 S S P G rade of Ag Sample Shape IV Sample of pre-dryer: Box 4 Fragment NA 0.741 Sample of pre-dryer: Box 5 Fragment NA 0.740 Sample of pre-dryer: Box 6 Fragment NA 0.747 Sample of pre-dryer: Box 7 Fragment NA 0.739 Sample of post-dryer: G (NA) Fragment NA 0.744 Post-dryer sample: H (549 ° F) (287 ° C) Fragment NA 0.732 Post-dryer sample: I (552 ° F) (288 ° C) Fragment NA 0.738 Preform sample: G (NA) Preform 8 0.721 Preform 25 0.712 Preform sample: H (549 ° F) (287 ° C) Preform 8 0.71 1 Preform 25 0.710 Preform sample: I (552 ° F) (288 ° C) Preform 8 0.714 Preform 25 0.716 Table 4 No SSP Water Grade As noted for the resin for CSD / beer bottles of Tables 1 and 2, the reduction in intrinsic viscosity of a polyester resin to be used in the manufacture of bottles for water is substantially lower when the resin is manufactured without polymerization in solid state, compared to a conventional resin that is manufactured without polymerization in solid state. For example, the change in intrinsic viscosity in the resin used in the process of the invention is about 0.01 deciliters / gram, while the change in intrinsic viscosity in the conventional resin is about 0.03 deciliters / gram. Two resins were tested for CSD / beer, for the qualification of the bottle, on 2 liter bottles. The preforms were injection molded into a 48 cavity mold, and the bottles were blow molded with stretch. Summary of Tests Both resins passed all qualification tests to date with comparable results. The test methods, specifications, and quantitative data are shown below. The stiffness test of the side wall has no specification. Table 5 Test Method No SSP SSP Impact of Fall Test 1 Pass Passes Test 2 Pasa Pasa Explosion Pressure Test 3 Pass Passes Test Method No SSP SSP Test 4 Pasa Pasa Rigidity of the lateral wall Test 5 Only Information only Thermal stability Test 6 Raisin Vertical load Test 7 Raisin Test 8 Pasa Pasa Volumes Test 9 Pasa Pasa Test 10 Pasa Pasa Stress cracking Test 11 Pasa Pasa Wall Pull Test 12 Only Side Only Information Information Top space of the Test 13 Pass Passes AA bottle Test 14 Pasa Pasa Permeation to C02 Test 15 Pasa Pasa Test procedures, specification, and results. A) Impact of fall - Test 1 24 carbonated bottles up to 4.2 + 0.1 gas volumes. 12 bottles conditioned at 70 ° F (21 ° C) and 12 bottles conditioned at 40 ° F (4.4 ° C), were dropped on the hot roll stainless steel plate at a height of 2 meters. Specification -without faults. Table 6 B) Fall impact - Test 2. 24 carbonated bottles at 4.00 + 0.05 volumes of gas. All bottles conditioned at 70 ° F (21 ° C) were dropped on an angle plate of stainless steel at a height of 6 feet (1.82 meters). 12 bottles were dropped vertically, and 12 bottles were dropped horizontally. Specification - without failures.

C) Extrusion pressure - Fall impact - Test 3. 12 bottles initially pressurized to 100 psig (7 kg / cm2), maintained for 13 seconds, and then the pressure was raised to 10 psi per second (0.7 kg / cm2) per second) up to 300 psig (21 kg / cm2) or until failure. Specification - the bottles must support a minimum of 100 psig (7 kg / cm2). Pass. Table 8 D) Explosion pressure - Impact of fall - Test 4. 6 bottles tested. No ramp or initial pressure support is specified. Specification - without failure to less than 135 psig (9.45 kg / cm2), and average - 3 (0.21) standard deviation > 135 psig (9.45kg / cm2) for the base failures, and > 120 psig (8.4 kg / cm2) for side panel failures. Pass. Table 9 Pressure (psig) No SSP SSP (kg / cm2) Average 178.3 (12.481) 190.0 (13.3) Pressure (psig) No SSP SSP (kg / cm2) Standard deviation 16.0 (1.12) 15.0 (1.05) Minimum 148.0 (10.36) 146.0 (10.22) Maximum 189.9 (13.273) 200.9 (14,063) Average - 3 (0.21) 130.4 (9.128) 145.0 (10.15) standard deviation E) Rigidity of the side wall - Test 5. 12 empty bottles. The label panel is deflected to 12 millimeters with an 8 millimeter round probe. The load is recorded at a deviation of 12 millimeters. It is repeated in four equal points on the bottle. There is no specification. Table 10 Load @ 12 mm (0.48 Not SSP SSP inches) (Ibf) (kgm) Average 222.81 (331,563) 230.16 (542,501) Standard deviation 6.5 (9,672) 6.1 (9,077) Maximum 234.09 (348.349) 242.68 (361.132) Minimum 207.78 (309.197) 210.47 (313.2) F) Thermal stability - Test 6. The required dimensions of the bottle are measured in 12 empty bottles. The same 12 bottles are carbonated up to 4.2 + 0.1 gas volumes. The bottles are stored at 100 ° F (37.7 ° C) for 24 hours. The required dimensions of the bottles are measured. Specification < 3 percent change in height, < 3 percent diameter change, change of < 28 millimeters (1.1 inches in the filling line, and final perpendicularity of <9 millimeters (0.35 inches)) All passed.

No SSP SSP Deviation Deviation Average Standard standard average Weight (grams) 50.1 0.06 50.1 0.04 Initial height (inches) 1865 0.002 11.863 0.003 (cm) (30.137 cm) (0.005 cm) (30.132 cm) (0.007 cm) % change in height 1.39% 0.001 1.40% 0.001 Change in line of 0.526 0.010 0.512 0.018 filling (inches) (cm) (1.336 cm) (0.025 cm) (1.3 cm) (0.045 cm) Tolerance of the base Initial (inches) (cm) 0.186 0.004 0.191 0.005 No SSP SSP Deviation Deviation Average Standard standard average (0.472 cm) (0.010 cm) (0.485 cm) (0.0127 cm) Finish (inches) (cm) 0.177 0.003 0.172 0.005 (0.444 cm) (0.007 cm) (0.436 cm) (0.0127 cm) Final perpendicularity 0.043 0.023 0.062 0.030 (inches) (cm) (0.109 cm) (0.058 cm) (0.157 cm) (0.0762 cm) % change in diameter % neck change 0.20% 0.001 0.18% 0.001 % change of the 1.36% 0.000 1 .36% 0.001 label top % change of the .65% 0.001 1 .59% 0.001 average label % change from 1.96% 0.001 1.84% 0.001 lower label Final carbonation 3.73 0.032 3.75 0.022 Base weight (grams) 15.9 0.236 15.9 0.184 Weight of the panel 20.1 0.200 20.2 0.162 No SSP SSP Deviation Deviation Average Standard standard average (grams) Shoulder weight 14.6 0.105 14.6 0.087 (grams) G) Vertical load - Test 7. 12 empty bottles. Stage 25 millimeters above the finish, and head speed at 20 inches / minute (50.8 centimeters / minute). Test until failure, and the maximum load is recorded. Average specification of 66 pounds (30 kilograms), and none less than 44 pounds (20 kilograms). Table 12 Maximum load No SSP SSP (Ibf) (kgm) Average 67.61 (100.61) 67.37 (100.293) Deviation 7,928 (11,797) 5,924 (8,815) standard Maximum 89.64 (133.393) 90.36 (134.464) Maximum load No SSP SSP (Ibf) (kgm) Minimum 57.37 (85.372) 60.70 (90.327) PASA PASA H) Vertical load - Test 8. 24 empty bottles aged for 72 hours. Head speed at 20 inches / minute (50.8 centimeters / minute). Test a deviation of 0.15. Specification of 35 pounds (15.8 kilograms), and average - 3 (0.21) (standard deviation) > 35 pounds (15.8 kilograms). Table 13 Compression load at a deviation of 0.15 Not SSP SSP inches (0.381 cm) (Ibf) (kgm) Average 62.3 (92,708) 62.3 (92,708) Standard deviation 8,400 (12.5) 6,714 (9,991) Maximum 86.4 (128,571) 84 (125) Minimum 51.5 (76.637) 53.8 (80.059) Compression load at a deviation of 0.15 Not SSP SSP inches (0.381 cm) (Ibf) (kgm) Average - 3 (021) 37.1 (55,208) 42.2 (62,797) (standard deviation) PASA PASA I) Volumes - Test 9. 12 bottles filled to the point of overflow and filling. Specification - no bottle > + 1 percent on volume, average < + 0.5 percent on volume. They passed. J) Volumes - Test 10. 6 bottles filled to the point of overflow and filling. Specification - no bottle > 17 milliliters or < 9 milliliters, average no of > 10 milliliters or < 0 milliliters. They passed. Table 14 No SSP SSP Overflow capacity Average (my) 2077.40 2076.70 Standard deviation 0.38 0.34 No SSP SSP Minimum 2076.82 2076.02 Maximum 2078.02 2077.22 Filling point capacity Average (mi) 2027.69 2026.27 Standard deviation 1.42 0.76 Minimum 2026.41 2025.61 Maximum 2031.02 2028.51 K) Tension cracking - Test 11. Each bottle is filled to the filling level with water at 22 ° F + 2 ° F (-5.5 ° C + 1 ° C), pressurized to 77 + 0.5 psig (5.39 + 0.035 kg / cm2), and it is maintained for 5 minutes. Each bottle is placed in a 0.2 percent NaOH solution, and the time to failure is recorded. They passed. Table 15 No SSP SSP Time to failure Average 1: 06: 26 1: 08: 20 No SSP SSP Standard deviation 0:54:48 0:51: 30 Minimum 3:00:00 2:51:23 Maximum 0:12:48 0:17:43 Filling point capacity Average (mi) 15.8 15.7 Standard deviation 0.2 0.2 Minimum 16.3 16.0 Maximum 15.5 15.3 Traction of the side wall - Test 12 Sections are cut from the side wall of the bottle, and cut into a dog bone pull bar. There are six samples of each sample. Three samples are cut in the axial direction of the bottles, and three samples in the radial direction of the bottle.

Ta b l a 1 6 No SSP SSP No SSP SSP Radio Axial Axial Radio Module (Young's cursor) Average 312405 322751 220720 162800 Standard deviation 15335.73187 22514.1 12932.8 9927.8 Maximum load Average 96,345 91.98 73.76 74 Standard deviation 0.4 1 .5 6.5 2.7 Stress @ Maximum load Average 31670.07 31967.46 27047.22 26870.67 Standard deviation 142.1 319.9 2188.8 1037.9 Traction @ Maximum load Average 38.26 35.9 214.32 265.16 Standard deviation 0.9 2.1 26.7 15.2 Stress @ Performance Average 31670.07 31967.46 13075.27 13245.95 No SSP SSP No SSP SSP Radio Axial Axial Radio Standard deviation 142.1 319.9 338.7 219.7 Stress @ Breakdown Average 40,505 37.84 216.66 267.94 Standard deviation 1.0 1.9 26.7 16.1 M) Top space of the AA bottles - Test 13. 6 bottles are purged after 24 hours with nitrogen. Specification < 5 micrograms / liter. They passed.

N) Upper space of AA bottles - Test 14. 6 bottles stored at 70 ° F (21 ° C) for 24 hours, and then purged with nitrogen. Specification < 3 micrograms / liter. They passed.

O) Permeation at C02 - Test 15. Carbonate with dry ice up to 4.0 + 0.1 gas volumes.

After 49 days, loss of 17.5 percent or less. Specification > 14 weeks They passed.

Table 19 In the following Tables 20 to 22 a comparison of the mold shrinkage between the non-SSP resins (eg, of the invention) and the SSP resins is tabulated.

Table 20 T 10 ° Line T 90 ° Line Diameter Partial partial partial ovality (ID) specification No No No No SSP SSP SSP SSP SSP SSP SSP SSP Nominal 1,080 1,080 1,080 1,080 0.856 0.856 Minimum 1,075 1,075 1,075 1,075 0.851 0.851 Maximum 1,085 1,085 1,085 1,085 0.861 0.861 Real Average 1,079 1,079 1,078 1,078 0.001 0.001 0.857 0.857 Maximum 1,077 1,077 1,077 1,077 0.000 0.001 0.855 0.856 Maximum 1,081 1,080 1,080 1,080 0.001 0.000 0.858 0.859 Difference 0.004 0.003 0.003 0.004 0.001 0.001 0.003 0.003 Deviation 0.0008 0.0005 0.0009 0.0010 0.0008 0.0012 standard Ta bl a 21 E 10 ° Line E 90 ° Line Diameter Partial partial partial ovality (ID) specification No No No No SSP SSP SSP SSP SSP SSP SSP SSP Nominal 0.982 0.982 0.982 0.982 1.101 1.101 Minimum 0.977 0.977 0.977 0.977 1.096 1.096 Maximum 0.987 0.987 0.987 0.987 1.106 1 .106 Real Average 0.982 0.982 0.981 0.980 0.001 0.001 1 .100 1 .100 Maximum 0.981 0.980 0.980 0.980 0.000 0.000 1.098 1 .098 Maximum 0.983 0.984 0.981 0.981 0.002 0.003 1.102 1 .101 Difference 0.001 0.003 0.002 0.002 0.002 0.003 0.003 0.003 Deviation 0.0005 0.0010 0.0005 0.0005 0.0008 0.0007 standard Table 22 The mold shrinkage data shows that the resin of the invention can provide the same mold shrinkage as conventional resins prepared with solid state polymerization.

Claims

1. A process for making an article configured from a solid polyester resin containing a polyester polymer, which comprises: forming the shaped article by melting and processing the polyester polymer without changing the intrinsic viscosity of the polyester polymer. polyester for more than 0.025 deciliters / gram; wherein the polyester polymer, prior to melting, has an intrinsic viscosity of 0.70 to 0.95, and wherein the polyester resin is made by a process that satisfies one or more conditions selected from the group consisting of: (i) ) without solid-state polymerization, (i) intrinsic high-viscosity melt polycondensation, and (iii) has a direct crystallization of the latent heat.

2. The process as claimed in claim 1, which further comprises: polymerizing a mixture comprising one or more diol units and one or more carboxylic acid units, or esters of a carboxylic acid, to form a molten resin that It contains polymerized monomer units, and solidifies the molten polymer to form the polyester resin.

3. The process as claimed in claim 1, in wherein the processing is at least one selected from the group consisting of injection molding, extrusion molding, sheet molding, reaction injection molding, injection blow molding, thermoforming, and stretch blow molding in one and Two steps.

4. The process as claimed in claim 1, wherein the polyester polymer has an intrinsic viscosity of 0.75 to 0.85 deciliters / gram prior to molding.

5. The process as claimed in claim 1, wherein both the polyester polymer prior to forming, and the polyester resin of the shaped article, have an intrinsic viscosity of about 0.80 deciliters / gram. The process as claimed in claim 1, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.02 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. The process as claimed in claim 1, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.015 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. The process as claimed in claim 1, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.01 deciliters / gram, in comparison with the intrinsic viscosity of the polyester polymer before melting. The process as claimed in claim 1, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.005 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. 10. The process as claimed in claim 1, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased is the same as the intrinsic viscosity of the polyester polymer before melting. The process as claimed in claim 1, wherein the processing is injection molding, and the shaped article is a preform or pattern, wherein the process further comprises: stretch blow molding the preform or the pattern. The process as claimed in claim 1, wherein the polyester resin comprises polymerized isophthalic acid units in an amount of 0 to 30 mole percent, based on the total number of moles of all monomeric dicarboxylic acid units in the polyester resin. The process as claimed in claim 1, wherein the polyester resin comprises polymerized units of isophthalic acid in an amount of 0 to 5 mole percent, based on the total number of moles of all monomeric dicarboxylic acid units in the polyester resin. The process as claimed in claim 1, wherein the polyester resin comprises polymerized units of isophthalic acid in an amount of 5 to 25 mole percent, based on the total number of moles of all monomeric units of dicarboxylic acid in the polyester resin. 15. The process as claimed in claim 1, wherein the solid polyester resin comprises polymerized units of isophthalic acid in an amount of 5 to 15 mole percent. 1

6. The process as claimed in claim 1, wherein the solid polyester resin comprises groups that react with terephthalic acid and ethylene glycol. The process as claimed in claim 1, wherein the polyester resin is in the form of at least one of fragments, granules, pellets, spheroidal particles, or ellipsoidal particles. 18. A molded article produced by a process comprising: forming the molded article by melting and processing a polyester resin containing a polyester polymer, without changing the intrinsic viscosity of the polyester polymer by more than 0.025 deciliters / gram; where the polyester polymer, before melting, has an intrinsic viscosity of 0.70 to 0.95, and wherein the polyester resin is made by a process that satisfies one or more conditions selected from the group consisting of: (i) without solid state polymerization, (ii) polycondensation of fusion of high intrinsic viscosity, and (iii) has a direct crystallization of latent heat. 19. The molded article as claimed in claim 18, wherein the processing is at least one selected from the group consisting of injection molding, extrusion molding, sheet molding, reaction injection molding, blow molding. by injection, thermoforming, and blow molding with one and two step stretch. 20. The molded article as claimed in claim 18, wherein the polyester polymer has an intrinsic viscosity of 0.75 to 0.85 deciliters / gram prior to molding. 21. The molded article as claimed in claim 18, wherein both the polyester polymer prior to forming, and the polyester of the shaped article, have an intrinsic viscosity of about 0.80 deciliters / gram. 22. The molded article as claimed in the claim 18, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.02 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. 23. The molded article as claimed in the claim 18, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.015 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. 24. The molded article as claimed in the claim 18, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by no more than 0.01 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. 25. The molded article as claimed in the claim 18, wherein the intrinsic viscosity of the polyester polymer of the shaped article is decreased by not more than 0.005 deciliters / gram, compared to the intrinsic viscosity of the polyester polymer before melting. 26. The molded article as claimed in the claim 18, wherein the intrinsic viscosity of the polyester polymer of the shaped article is the same as the intrinsic viscosity of the polyester polymer before melting. 2

7. The molded article as claimed in claim 18, wherein the processing is injection molding, and the shaped article is a preform or pattern, wherein the process further comprises: stretch blow molding the preform or the pattern . 2

8. The molded article as claimed in the claim 18, wherein the polyester resin comprises polymerized isophthalic acid units in an amount of 0 to 30 mole percent, based on the total number of moles of all monomeric dicarboxylic acid units in the polyester resin. 2

9. The molded article as claimed in claim 18, wherein the polyester resin comprises polymerized units of isophthalic acid in an amount of 0 to 5 mole percent, based on the total number of moles of all monomeric acid units. dicarboxylic in polyester resin. The molded article as claimed in claim 18, wherein the polyester resin comprises polymerized units of isophthalic acid in an amount of 5 to 25 mole percent, based on the total number of moles of all monomeric acid units dicarboxylic in polyester resin. 31. The molded article as claimed in claim 18, wherein the solid polyester resin comprises polymerized units of isophthalic acid in an amount of 5 to 15 mole percent, based on the total number of moles of all monomeric units of dicarboxylic acid in the polyester resin. 32. The molded article as claimed in claim 18, wherein the solid polyester resin comprises groups that they react with terephthalic acid and ethylene glycol. 33. The molded article as claimed in claim 18, wherein the polyester resin is in the form of at least one of fragments, granules, pellets, spheroidal particles, or ellipsoidal particles. 34. A process for the formation of an article molded from a polyester resin containing a polyester polymer, which comprises: forming the molded article by melting and processing the polyester resin, without drying or partially drying the polyester resin before melting and processing; wherein the polyester polymer has an intrinsic viscosity of 0.7 to 0.95 deciliters / gram before melting, and the intrinsic viscosity of the polyester polymer after melting and processing has decreased by no more than 0.05 deciliters / gram, and in wherein the polyester resin is made by a process that satisfies one or more conditions selected from the group consisting of: (i) without solid state polymerization, (ii) intrinsic high viscosity melt polycondensation, and (iii) has a direct crystallization of the latent heat. 35. A process for forming an article molded from a solid polyester resin containing a polyester polymer, which comprises: forming the molded article by melting and processing a composition comprising the polyester resin and one or more additives, wherein the polyester polymer has an intrinsic viscosity of 0.7 to 0.95 deciliters / gram before melting and processing, and the intrinsic viscosity of the polyester polymer decreases by not more than 0.05 deciliters / gram after molding and processing, and wherein the polyester resin is made by a process that satisfies one or more conditions selected from the group consisting of (i) without polymerization in the solid state, (ii) fusion polycondensation of high intrinsic viscosity, and (iii) has a direct crystallization of the latent heat. 36. The process as claimed in claim 35, wherein the composition comprises one or more additives selected from the group consisting of an acetaldehyde scavenger and an acetaldehyde scavenger.